Handbook of Polymer Foams

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Handbook of Polymer Foams

Editor: David Eaves

Handbook of Polymer Foams

Editor: David Eaves C. Vasile

Rapra Technology Limited Shawbury, Shrewsbury, Shropshire, SY4 4NR, United Kingdom Telephone: +44 (0)1939 250383 Fax: +44 (0)1939 251118 http://www.rapra.net

First Published in 2004 by

Rapra Technology Limited Shawbury, Shrewsbury, Shropshire, SY4 4NR, UK

©2004, Rapra Technology Limited

All rights reserved. Except as permitted under current legislation no part of this publication may be photocopied, reproduced or distributed in any form or by any means or stored in a database or retrieval system, without the prior permission from the copyright holder. A catalogue record for this book is available from the British Library.

Every effort has been made to contact copyright holders of any material reproduced within the text and the authors and publishers apologise if any have been overlooked. Cover photograph reproduced with permission from EVC

ISBN: 1-85957-388-6

Typeset, printed and bound by Rapra Technology Limited Cover printed by The Printing House, Crewe, UK

Contents

Contents Preface .................................................................................................................. ix 1

Foam Fundamentals ........................................................................................ 1 1.1

Introduction ........................................................................................... 1

1.2

Foam Structure ...................................................................................... 1

1.3

Foam Properties ..................................................................................... 3 1.3.1

Compression Properties ............................................................. 3

1.3.2

Energy Absorption Properties .................................................... 5

1.3.3

Thermal Properties .................................................................... 6

References ....................................................................................................... 8 2

Blowing Agents ............................................................................................... 9 2.1

Introduction ........................................................................................... 9

2.2

Physical Blowing Agents ...................................................................... 10

2.3

2.2.1

Selection Criteria for Physical Blowing Agents ........................ 10

2.2.2

Halogenated Hydrocarbons ..................................................... 13

2.2.3

Hydrocarbons (HC) ................................................................. 20

2.2.4

Inert Gases ............................................................................... 22

2.2.5

Other Physical Blowing Agents ................................................ 24

2.2.6

Blends of Physical Blowing Agents ........................................... 24

2.2.7

Encapsulated Physical Blowing Agents .................................... 25

2.2.8

Physical Blowing Agent by Foam Type and Application .......... 25

Chemical Blowing Agents .................................................................... 25 2.3.1

Selection Criteria for Chemical Blowing Agents ...................... 29

2.3.2

Exothermic CBA ...................................................................... 30

2.3.3

Endothermic CBA .................................................................... 32

2.3.4

Endo/Exo Blends ...................................................................... 33 i

Handbook of Polymer Foams

References ..................................................................................................... 34 3

Expanded Polystyrene: Development, Processing, Applications and Key Issues ............................................................................................... 37 3.1

Introduction ......................................................................................... 37 3.1.1

Development of Expanded Polystyrene (EPS) .......................... 37

3.2

Manufacture of Expanded Polystyrene Mouldings .............................. 38

3.3

Applications for Expanded Polystyrene Packaging ............................... 41

3.4

3.5

3.6

3.3.1

Packaging ................................................................................ 41

3.3.2

Construction ............................................................................ 42

3.3.3

Other Applications .................................................................. 43

3.3.4

Novel Applications .................................................................. 44

Properties of EPS ................................................................................. 44 3.4.1

Mechanical Performance .......................................................... 45

3.4.2

Thermal Insulation .................................................................. 45

3.4.3

Chemical Properties ................................................................. 46

3.4.4

Recent Research on Properties of EPS: Value for Fruit and Vegetables ................................................................ 46

Global Structure of Markets and Companies ....................................... 47 3.5.1

Europe ..................................................................................... 47

3.5.2

Asia .......................................................................................... 48

3.5.3

USA ......................................................................................... 49

Key Issues Facing the EPS Industry ...................................................... 50 3.6.1

Fire .......................................................................................... 50

3.6.2

Recycling ................................................................................. 51

3.6.2

Alternatives to Mechanical Recycling ...................................... 53

Further Information ...................................................................................... 54 4

Rigid Polyurethane Foams ............................................................................ 55 4.1

ii

Introduction ......................................................................................... 55

Contents

4.2

Materials.............................................................................................. 57 4.2.1

Polyols ..................................................................................... 57

4.2.2

Isocyanates .............................................................................. 60

4.2.3

Blowing Agents ........................................................................ 62

4.2.4

Other Additives ....................................................................... 71

4.3

Manufacturing Processes for Rigid Polyurethane Foam ....................... 73

4.4

Recycling Processes for Rigid Polyurethane Foam ............................... 75

4.5

Properties of Rigid Polyurethane Foams .............................................. 76

4.6

Applications ......................................................................................... 78 4.6.1

Applications in Construction ................................................... 78

4.6.2

Applications in the Appliance Industry .................................... 80

References ..................................................................................................... 82 5

Flexible Polyurethane Foam .......................................................................... 85 5.1

Introduction ......................................................................................... 85

5.2

Chemistry ............................................................................................ 85

5.3

Starting Materials ................................................................................ 87 5.3.1

Isocyanate ................................................................................ 88

5.3.2

Polyol ...................................................................................... 88

5.3.3

Water ....................................................................................... 90

5.3.4

Surfactant ................................................................................ 90

5.3.5

Catalyst ................................................................................... 91

5.3.6

Colorants ................................................................................. 92

5.3.7

Antioxidants ............................................................................ 92

5.3.8

Light Stabilisers ...................................................................... 93

5.3.9

Flame Retardants ..................................................................... 93

5.3.10 Adhesion Promoters ................................................................. 94 5.3.11 Other Additives ....................................................................... 94 5.4

The Foaming Process ........................................................................... 94

iii

Handbook of Polymer Foams

5.5

5.6

5.4.1

Raw Material Conditioning ..................................................... 95

5.4.2

Mixing ..................................................................................... 95

5.4.3

Growth .................................................................................... 96

5.4.4

Cell Opening ............................................................................ 97

5.4.5

Cure ......................................................................................... 98

Manufacturing Equipment ................................................................... 99 5.5.1

Storage and Delivery .............................................................. 100

5.5.2

Mixing ................................................................................... 101

5.5.3

Foam Rise and Cure .............................................................. 101

5.5.4

Innovations ............................................................................ 103

Foam Characterisation ....................................................................... 104 5.6.1

Density .................................................................................. 104

5.6.2

Hardness ................................................................................ 104

5.6.3

Resilience ............................................................................... 105

5.6.4

Porosity ................................................................................. 106

5.6.5

Strength Properties ................................................................. 106

5.6.6

Cell Structure ......................................................................... 107

5.6.7

Environmental Stability ......................................................... 107

5.6.8

Fatigue ................................................................................... 108

5.6.9

Compression Set .................................................................... 108

5.6.10 Flammability .......................................................................... 108 5.7

FPF Markets ...................................................................................... 109 5.7.1

Transportation ....................................................................... 110

5.7.2

Comfort ................................................................................. 110

5.7.3

Carpet Cushion ...................................................................... 110

5.7.4

Packaging .............................................................................. 111

5.7.5

Specialty Applications ............................................................ 111

5.8

Environmental Issues ......................................................................... 111

5.9

Organisations .................................................................................... 113

References ................................................................................................... 114 iv

Contents

6

Rigid PVC Foam ......................................................................................... 123 6.1

Introduction ....................................................................................... 123

6.2

Foam Extrusion ................................................................................. 124

6.3

6.2.1

Basic Principles ...................................................................... 125

6.2.2

Extrusion Processes ................................................................ 126

6.2.3

Effect of Processing Conditions ............................................. 131

Foam Formulation Technology .......................................................... 132 6.3.1

Blowing Agents ...................................................................... 133

6.3.2

Processing Aids ...................................................................... 138

6.3.3

Type of PVC .......................................................................... 140

6.3.4

Stabilisers ............................................................................... 140

6.3.5

Lubricants .............................................................................. 141

6.3.6

Typical Formulations ............................................................. 141

6.4

Properties ........................................................................................... 143

6.5

Novel Processes and Applications ...................................................... 145

6.6

6.5.1

Recycling ............................................................................... 145

6.5.2

Microcellular Foam ............................................................... 146

6.5.3

Foamed Composites ............................................................... 147

Summary ............................................................................................ 147

References ................................................................................................... 148 7

Flexible PVC Foams .................................................................................... 155 7.1

Introduction ....................................................................................... 155

7.2

Flexible Foam Types and PVC Types ................................................. 155 7.2.1

Flexible Foams Based on Suspension PVC ............................. 155

7.2.2

Flexible Foams Based on Dispersion or Paste Resins ............. 156

7.2.3

Chemically Blown Foams from PVC Plastisols: Fundamentals ........................................................................ 156

7.2.4

PVC Resins used in Plastisol Foam Formation ....................... 160

v

Handbook of Polymer Foams

7.3

7.2.5

Mineral Fillers ....................................................................... 161

7.2.6

Pigments ................................................................................ 162

7.2.7

Liquid Plasticiser .................................................................... 162

7.2.8

Blowing Agent Type and Level ............................................... 165

Products Utilising Foamed Plastisols .................................................. 166 7.3.1

Floorings and Carpet Backings .............................................. 166

7.3.2

Wallcoverings ......................................................................... 168

7.3.3

Synthetic Leather ................................................................... 169

7.3.4

General Foams ....................................................................... 170

References ................................................................................................... 171 8

vi

Polyolefin Foams ......................................................................................... 173 8.1

Introduction ....................................................................................... 173

8.2

Manufacturing Processes and Materials ............................................. 174 8.2.1

Extruded Non-Crosslinked Foam .......................................... 174

8.2.2

Expanded (Non-Crosslinked) Polyolefin Beads ...................... 177

8.2.3

Extruded Crosslinked Foam - Processes ................................. 179

8.2.4

Press Moulded Crosslinked Foam Process ............................. 186

8.2.5

Injection Moulded Foam Process ........................................... 189

8.2.6

The Nitrogen Autoclave Process ............................................ 189

8.2.7

Recycling Processes ................................................................ 193

8.2.8

Post Manufacturing Operations ............................................. 194

8.3

Properties of Polyolefin Foams .......................................................... 195

8.4

Applications ....................................................................................... 197

8.5

Foam Specifications ........................................................................... 200 8.5.1

Packaging .............................................................................. 200

8.5.2

Automotive ............................................................................ 201

8.5.3

Furnishings ............................................................................ 201

8.5.4

Buoyancy ............................................................................... 201

Contents

8.6

8.5.5

Aerospace .............................................................................. 201

8.5.6

Construction .......................................................................... 202

8.5.7

Toys ....................................................................................... 202

8.5.8

Food contact .......................................................................... 202

Markets ............................................................................................. 202

References ................................................................................................... 203 9

Latex Foam ................................................................................................. 207 9.1

Introduction ....................................................................................... 207

9.2

Dunlop Process .................................................................................. 208 9.2.1

Batch Process ......................................................................... 209

9.2.2

Selecting a Formulation for Latex Compounds ...................... 215

9.2.3

Selection of Other Compounding Ingredients ........................ 217

9.2.4

Continuous Process for Latex Foam Production .................... 229

9.3

Talalay Process ................................................................................... 230

9.4

Troubleshooting in Latex Foam Manufacture .................................... 235

9.5

Testing ............................................................................................... 236

9.6

9.5.1

Compression Set .................................................................... 236

9.5.2

Indentation Hardness ............................................................. 236

9.5.3

Flexing Resistance .................................................................. 238

9.5.4

Density .................................................................................. 238

9.5.5

Metallic Impurities ................................................................. 238

Important Uses of Latex Foam........................................................... 238 9.6.1

Transportation ....................................................................... 238

9.6.2

Furniture ................................................................................ 239

9.6.3

Special Uses ........................................................................... 239

References ................................................................................................... 239 10 Microcellular Foams ................................................................................... 243

vii

Handbook of Polymer Foams

10.1 Introduction ....................................................................................... 243 10.2 Processing of Microcellular Foams .................................................... 244 10.2.1 The Solid-State Batch Process ................................................ 244 10.2.2 The Semi-Continuous Process ................................................ 247 10.2.3 Extrusion and other Processing Methods ............................... 248 10.3 Properties of Microcellular Foams ..................................................... 249 10.4 Current Research Directions .............................................................. 254 10.4.1 Microcellular Materials for Construction .............................. 254 11.4.2 Open-Cell (Porous) Microcellular Foams ............................... 255 10.4.3 Sub-Micron Foams and Nanofoams ...................................... 256 10.5 Commercial Opportunities ................................................................ 261 References ................................................................................................... 262 Abbreviations .................................................................................................... 269 Contributors ...................................................................................................... 275 Index ................................................................................................................. 277

viii

Preface

Preface

The use of polymer foams is extremely widespread. Indeed, it is difficult to think of a single industry where polymer foams do not have a significant application. They can be found for example in sports and leisure products, in military applications, in vehicles, in aircraft, and in the home. Most people will encounter polymer foams every day in one form or another, whether it be in furniture, in packaging, in their car, in refrigerator insulation, or in some other common application. Although naturally occurring polymer foams have been known for a long time, (e.g., sponges, cork), synthetic polymer foams have only been introduced to the market over the last fifty years or so. The development of a new polymer has usually been quickly followed by its production in an expanded or foam form owing to the unique and useful properties which can be realised in the expanded state. Compressibility, thermal insulation and, of course, low density/lightness are all enhanced in a foam as compared with the original polymer. Such properties can be tailored to meet particular requirements and can increase substantially the potential applications of a polymer. Foaming technology and the properties of expanded materials should therefore be of interest to all those working in the polymer industry. This Handbook aims to review the chemistry, manufacturing methods, properties and applications of the synthetic polymer foams used in most applications. In addition, a chapter is included on the fundamental principles which apply to all polymer foams. There is also a chapter on the blowing agents used to expand polymers, blowing agents having undergone considerable change and development in recent years in order to meet the requirements of the Montreal Protocol in relation to the reduction and elimination of chloroflurocarbons (CFC) and other ozone depleting agents. A chapter is also included on microcellular foams - a relatively new development where applications are still being explored. Each chapter has references to facilitate further exploration of the subject. I am very much indebted to my co-authors for their contributions. They all have substantial expertise on their particular topics and have given considerable time to the production

ix

Handbook of Polymer Foams of their chapters. I am also indebted to the staff at RAPRA for their work in pursuing and assembling the various contributions to produce the final composite, especially Frances Powers (Commissioning Editor), Claire Griffiths (Editorial Assistant) and Sandra Hall (Graphic Designer).

David Eaves Harbury, UK November 2003

x

Foam Fundamentals

1

Foam Fundamentals David Eaves

1.1 Introduction Although polymer foams are based on a wide variety of materials and are manufactured in many different forms, there are some principles and concepts which apply to all foams. These have been reviewed in depth elsewhere [1, 2]. Since these concepts are useful in understanding the relationships between polymer properties and foam structure and can facilitate the prediction of the physical behaviour of foams in typical applications, this chapter provides a summary of some of these fundamentals.

1.2 Foam Structure Most foams are formed by a process involving nucleation and growth of gas bubbles in a polymer matrix (exceptions being syntactic foam where micro-beads of encapsulated gas are compounded into a polymer system, and latex foam). As the bubbles grow, the foam structure changes through stages which may be described as follows: •

Initially, small dispersed spherical bubbles are generated in a liquid matrix, with a small reduction in density.

•

Whilst the bubbles grow but still remain spherical, the lowest foam density is achieved when bubbles reach close packed structure.

•

Further growth and lower foam density then involves distortion of cells to form polyhedral structures, sometimes idealised as pentagonal dodecahedrons.

•

Viscous and surface tension effects subsequently cause material to flow towards intersecting cell elements to form junctions of tricuspid cross-section.

•

A final stage may involve rupture of cell walls to result in an open cell foam.

1

Handbook of Polymer Foams Depending on the degree of expansion and the particular formulation, foams can have any or a combination of these structures. A comprehensive characterisation may therefore include a measure of: a) Foam density - usually expressed as kg/m3. A more fundamental measure is relative density (φ), i.e., density of foam (ρf) compared with density of the original polymer (ρs), or φ = ρf/ρs Relative density may also be regarded as the volume fraction of polymer in a foam. Low density foams are generally regarded as those with volume fraction of polymer R-NCO + HCl

(4.2)

More recently phosgene free methods have been developed, for example, reductive carbonylation of a nitro compound in the presence of an alcohol to produce a urethane which thermally dissociates to give an isocyanate:

60

Rigid Polyurethane Foams R-NO2 + 3CO + R´-OH ————> R-NH-CO-O-R´ + 2CO2

(4.3)

R-NH-CO-O-R´ ————> R-NCO + R´-OH

(4.4)

Several other phosgene free routes are also available. MDI is obtained initially as a mixture of di-cyclic monomeric MDI (MMDI) and polycyclic polyisocyanates (PMDI) with approximate proportions as shown in Table 4.4. MMDI is separated from the polymeric form by distillation and exists in two isomeric forms: 2,4-MDI and 4,4-MDI. Both are solid materials at room temperature (melting point 38 °C), the latter with a tendency to dimerise. The main applications for MMDI are prepolymers for flexible foams, shoe soles and thermoplastic polyurethanes (TPU). The more important form of MDI in terms of volume is PMDI which is a mixture of isocyanates with two or more aromatic rings remaining in the distillation residue. PMDI is a yellow to dark brown material, liquid at room temperature (melting point less than 10 °C) with a higher functionality than MMDI but, owing to the lower NCO content, of reduced reactivity. The higher functionality of PMDI facilitating the production of a rigid, crosslinked, network coupled with the highly aromatic character which contributes to flame resistance, makes PMDI the isocyanate of choice for most rigid polyurethane foams. TDI, produced from toluene diamine, is a colourless liquid commercially available as a mixture of the 2,4 and 2,6 isomers in the ratio of 20:80 (TDI T-80) or 65:35 (TDI T-65). Its main use is in the production of flexible polyurethane foams. Other isocyanates are available, such as, 1,6-hexamethylene diisocyanate, isophorone diisocyanate and tetra-methyl xylene diisocyanate. These are used for special applications such as light, weather and heat resistant coatings, but have little application as rigid foams.

Table 4.4 Composition of MDI as manufactured 2 ring monomeric MDI

48%

3 ring compounds

27%

4 ring compounds

5%

5 ring compounds

4%

Higher homologues

16%

Source: [5]

61

Handbook of Polymer Foams Isocyanates may be modified by including linkages such as allophanate, carbodiimide and isocyanate to control reactivity and lower vapour pressure. They may also be ‘blocked’ by reaction with compounds containing labile hydrogen atoms, e.g., phenols and nitrophenols. Blocked isocyanates have the advantage of being inert at room temperature but liberate free isocyanate groups for reaction when the temperature is raised. This technology has application in heat activated coatings but again is not commonly used for rigid foam production.

4.2.3 Blowing Agents Rigid polyurethane foams produced in the 1960s used CFC-11 (trichlorofluoromethane) as the principle blowing agent. The type of blowing agent used, which is retained as vapour in the closed cells of the foam, is a major factor controlling the thermal conductivity and such foams had conductivity values around 17 mW/m.K. With the introduction of aromatic-based polyethers and esters, and further work adjusting formulations, conductivities down to 15 mW/m.K were achieved and these later foams also showed good long-term retention of the low conductivity values. Development work at that time aimed for even further improvements in insulation to achieve satisfactory performance from increasingly thinner, and hence more cost effective, sheets. However, by the late 1980s, CFC-11 and CFC-12 (dichlorodifluoromethane) had been recognised as chemicals very effective at depleting the protective ozone layer in the atmosphere and were environmentally unacceptable. This resulted in the introduction in 1987, of the now well known Montreal Protocol in which international action was agreed to combat the effects of these substances. The Protocol came into force in 1989 and provided a timetable whereby, in developed countries, use of CFC would be phased out by 1st January 1996. In Europe, this was advanced to 1st January 1995 with the adoption of regulation EC3093/94. Since it was recognised that products like rigid PU foams made an important environmental contribution through their insulative qualities which reduce energy requirements and hence carbon dioxide emissions, the phase-out arrangements were of a gradual nature with an interim period. During this time, CFC could be replaced with ‘transitional substances’ of much reduced ozone depletion potential (ODP) which would be phased out in the period 2003-2015, or earlier if possible. The phase-out schedule agreed at the Montreal meeting of September 1997 for ozone depleting substances (ODS) is shown in Table 4.5 (developed countries) and Table 4.6 (developing countries). The Annexes refer to various classes of ODS with CFC-11 and CFC-12 in Annex A and hydrochlorofluorocarbon (HCFC) in Annex C, Group 1. There are some exemptions for essential use but these do not include use for blowing agents. 62

consumption phase-out of ODS Rigid Polyurethane Foams

Table 4.5 Consumption phase-out of ODS in developed countries Date

Central Measure

1st July 1989

Freeze Annex A (CFC)

1st January 1992

Freeze of halons

1st January 1993

• Annex B CFC reduced by 20% from 1989 levels • Freeze of methyl chloroform

1st January 1994

• Annex B: CFC reduced by 75% from 1989 levels • Annex A: CFC reduced by 75% from 1986 levels • Halons phased out • Methyl chloroform reduced by 50%

1st January 1995

• Methyl bromide frozen at 1991 levels • Carbon tetrachloride reduced by 85% from 1989 levels

1st January 1996

• HBFC phased out • Carbon tetrachloride phased out ª Annex A and B: CFC phased out • Methyl chloroform phased out • HCFC frozen at 1989 level + 2.8% of 1989 consumption of CFCs (base level)

1st January 1999

Methyl bromide reduced by 25% from 1991 levels

1st January 2001

Methyl bromide reduced by 50% from 1991 levels

1st January 2003

Methyl bromide reduced by 70% from 1991 levels

1st January 2004

HCFC reduced by 35% below base levels

1st January 2005

Methyl bromide phased out

1st January 2010

HCFC reduced by 65%

1st January 2015

HCFC reduced by 90%

1st January 2020

HCFC phased out, allowing for a service tail of 0.5% until 2030 for existing refrigerators and air conditioning equipment

HBFC: Hydro bromo fluorocarbons

Some developed countries including USA, Japan and the European Union (EU) have brought these targets forward. The EU has agreed that from 1st January, 2003, the use of HCFC in appliances and sandwich panels (except for insulation trucks) will be prohibited. From 1st January, 2004, prohibition extends to HCFC in other rigid foams

63

consumption phase-out of ODS Handbook of Polymer Foams

Table 4.6 Consumption phase-out of ODS in developing countries Date

Central Measure

1st July 1999

Freeze of Annex A CFC at 1995-1997 average levels

1st January 2002

• Freeze of halons at 1995-1997 average levels • Freeze of methyl bromide at 1995-1998 average levels

1st January 2003

• Annex B: CFC reduced by 20% from 1998-2000 average levels • Freeze of methyl chloroform at 1998-2000 average levels

1st January 2005

• Annex A: CFC reduced by 50% from 1995-1997 average levels • Halons reduced by 50% • Carbon tetrachloride reduced by 85% from 1998-2000 average levels • Methyl chloroform reduced by 30% from 1998-2000 average levels

1st January 2007

• Annex A: CFC reduced by 85% from 1995-1997 average levels • Annex B: CFC reduced by 85% from 1998-2000 average levels

1st January 2010

• CFC, Halons and CCl4 phased out • Methyl chloroform reduced by 75% from 1998-2000 average levels

1st January 2015

Methyl chloroform phased out

1st January 2016

Freeze of CFC at baseline figure of year 2015 average levels

1st January 2040

HCFC phased out

Source: [6]

such as spray, block and polyisocyanurate. An EU amendment to bring dates forward by another 12 months narrowly failed. The replacement of CFC has been the main development target of the rigid PU foam industry since 1986, and the repercussions of this, in optimising the performance of alternative non CFC formulations and moving away from transitional substances, continue. The success of work to replace CFC can be judged from Table 4.7, which shows the use of ozone depleting substances by the European foam industry since 1986.

64

Ozone depleting substances Rigid Polyurethane Foams

Table 4.7 Use of ozone depleting substances by the European foam industry Year

ODP (000s weighted tonnes)

1986

63

1987

67

1988

70

1989

70

1990

69

1991

51

1992

39

1993

22

1994

4

1995

4

1996

4

1997

4

1998

4

1999

4

Derived from data in [7]

The desirable characteristics of blowing agents for rigid PU foams are well understood, and are: •

Boiling point in the range –20 to +30 °C

•

Good solubility in the foam precursors

•

Poor solubility in the foam polymer

•

Low thermal conductivity of gas/vapour

•

Low diffusion rate of gas/vapour through the polymer (for long-term retention in the cells)

65

Handbook of Polymer Foams •

Zero ODP

•

Low flammability both as liquid and gas

•

Chemically inert

Initial work on alternatives resulted in the development of so-called 50% reduced CFC-11 systems which were adopted in the late 1980s [8]. These systems were very much an interim measure to meet the short term reductions of ODP substances specified by the Montreal Protocol. Development to meet the longer term requirements have resulted essentially in two types of blowing agent - HCFC (such as HCFC-141b) and hydrocarbons (such as n-pentane). Some characteristics of these substances are shown in Table 4.8.

Table 4.8 Characteristics of some alternative blowing agents Property

CFC-11

HCFC-141b

HFC-134a

CO2

n-pentane

cyclopentane

Formula

CCl3F

CH3CCl2F

CH2FCF3

CO2

C5H12

C5H10

Molecular weight

13 7

117

102

44

72

70

Boiling point (°C)

24

32

-26.5

-

36

49

0.082

0.053

Vapour pressure at 30 °C (MPa)

0.08

Vapour conductivity at 20 °C (mW/m.K)

8

9

14

15

13

11

Flash point (°C)

none

none

none

none

< -50

-42

Explosion limits in air (% by volume)

none

7.4-15.5

none

none

1.4-7.8

1.4-8.0

TLV (ppm)

1000

500

1000

-

1000

600

1.0

0.11

0

0

0

0

good

good

good

poor

good

good

ODP (cf CFC-11) Permanency in cells

Adapted from data in [7], with permission from Rapra Technology HFC: Hydrofluorocarbon TLV: Threshold limit value

66

Rigid Polyurethane Foams From Table 4.8 it may be seen that there is no ideal replacement for CFC-11. HCFC141b, whilst giving a very substantial reduction in ODP does not have a zero ODP factor and the Protocol requires eventual phase-out. In addition, thermal conductivity is slightly worse and mixtures with air are explosive (within defined limits). HFC, such as HFC134a, do have zero ODP and are acceptable under the Protocol (although they do have some potential for global warming). They are non-flammable and non-explosive, but thermal conductivity is significantly worse than CFC-11. Carbon dioxide is a very safe gas to work with, but again has worse thermal insulation properties which are exacerbated by the impermanence of the gas in the cells, leading to a gradual deterioration in insulation and some dimensional stability problems. It also contributes to global warming, so is not totally environmentally acceptable (though it may be argued that environmental deterioration due to the use of carbon dioxide as a blowing agent is vastly outweighed by contributions of carbon dioxide to the atmosphere from transport and energy production). Hydrocarbons have zero ODP (and negligible global warming potential) and hence offer a permanent solution to Protocol requirements, but they are flammable and form explosive mixtures with air. Compared with CFC-11 there is also a significant worsening of thermal insulation. In addition to the intrinsic properties of alternative blowing agents and the properties they consequently impart to the foam, effect on processing is also very important. Whereas HCFC-141b is essentially a drop-in agent which can be run with relatively minor adjustments on conventional machines, engineering solutions have had to be found to introduce gases and flammable blowing agents. Worldwide, no single blowing agent technology has been universally adopted [9]. The phase-out of CFC has resulted in a broad diversification of rigid PU foam processes using HCFC-141b, HCFC-22 with HCFC-142b, HFC-134a, pentane isomers and carbon dioxide. HCFC-141b is currently used in the manufacture of metal faced sandwich boards. Whilst it is ‘drop-in’ technology, greater control of processing is needed and some dimensional stability problems require higher foam densities. This technology has been in place for some time producing foams of density 38-43 kg/m3 (continuous process) and 41-43 kg/ m3 discontinuous. This is the main technology adopted in the USA owing to the large emphasis placed on energy conservation and the environmental penalties exacted for units with large energy demands. HCFC-141b has also been used for appliance insulation applications, (e.g., in the Pacific area), where it is also a ‘drop in’ technology in terms of the foaming process. However, the solvent effect of HCFC-141b on acrylonitrile-butadiene-styrene or high impact polystyrene thermoplastics has required the development of special liners to prevent cracking, resulting in extra cost. In both appliance and board insulation, the early phase67

Handbook of Polymer Foams out of HCFC-141b in such countries as USA, Japan and the EU will considerably reduce its use. HCFC-22/142b has been used particularly in Germany and offers advantages of good dimensional stability but with some worsening of thermal conductivity. HFC-134a, in low amount, has been used industrially in both the continuous and discontinuous processes. The substance is dosed into the high pressure polyol stream in continuous operations, or used in a fully saturated polyol component in discontinuous operations. Carbon dioxide water blown foams are also produced successfully by panel manufacturers, with densities ranging from 43 to 48 kg/m3. The inferior long-term ageing (loss of insulation) due to diffusion of carbon dioxide from the cells can be mitigated by use of an impervious facing. It is claimed that with such composites, thermal conductivity remains practically unchanged for a long time in the largest part of the panel [9]. A recent variant is the use of liquid carbon dioxide to partially replace water. The carbon dioxide is metered and fed in the high pressure polyol stream at a level of some 3 pbw. Some process advantages have been described, but engineering modifications are necessary to handle and meter the gas and the technology has not so far been used industrially for sandwich panels due to unclear economics in comparison with all water blown technology. The use of pentane - either n-pentane or cyclopentane - is now widespread in the European industry for the production of metal faced rigid PU panels. Technology has been developed to deal with the problems imposed by flammability, including membrane pumps for dosing and static mixers for blending with the polyol stream. Strict precautions are taken to ensure there is no build-up of explosive vapours, and continuous monitoring ensures vapour levels are maintained below 10% of the lower explosion limit. Ignition sources must be eliminated. With these precautions, pentane can be used safely and the first equipment for production of pentane blown rigid PU was introduced in 1990. Pentane may be partially emulsified (and not solubilised) in the polyol stream depending on the amount used and its solubility in the polyol. Blends of n-pentane and methylene chloride have also been used and have some advantage since methylene chloride in non-flammable. However, concerns over environmental and toxicity issues have prevented any significant use as a blowing agent. Pentane has some advantages over other blowing agents - it has zero ODP, poor solubility and low permeability in the PU matrix, gives acceptable foam insulation values (though inferior to those of CFC foams) and low price. The obvious disadvantage is its flammability. In addition to the necessity of introducing new equipment to provide adequate operating safety there is an adverse contribution of the hydrocarbons to the foam combustion behaviour, and inferior fire performance results. This may be combated by the introduction of additional fire retardants or, as indicated previously, by use of

68

comparative costs Rigid PU foam Rigid Polyurethane Foams polyisocyanurate foam chemistry, but this results in a cost penalty. Thus, the economics of pentane blown foam versus other technologies depends on the fire classification requirements. Some data given by Bertucelli and co-workers are shown in Table 4.9. Cyclopentane and n-pentane (or n-i pentane blends) are sufficiently different in properties to give rise to significant differences in processing and foam properties. Where a homogeneous blend is preferable (discontinuous processes) cyclopentane is preferred, and this also provides optimum thermal properties. N-pentane has lower cost and gives a lower foam density, resulting in better foam economics. There is significant work still ongoing in the polyurethane industry to fully replace HCFC141b in developed countries. Whilst pentane and carbon dioxide technologies are already in place, neither provides the advantageous process and product characteristics given by CFC-11. For a few years now, HFC-245fa (structure CF3-CH2-CHF2) and HFC-365mfc (structure CF3-CH2-CF2-CH3) have been identified as the leading candidates. It has been reported by Zipfel and co-workers [12] that whilst neither of these substances entirely matches CFC-11, a blend of HFC-365mfc with either HFC-134a or HFC-245fa provides a non-flammable blowing agent with good thermal insulation performance and a convenient boiling point in the range 20-25 °C. Such a blend would provide a ‘drop-in’ replacement for HCFC-141b (and CFC-11), but is the most expensive option of those under examination. A further possibility for the future is an azeotropic blend of HFC365mfc with any of the three pentane isomers (n, i, or cyclo). Although these azeotropes are flammable, they do provide a more cost effective solution than use of HFC-365mfc alone, and results show good thermal insulation values for foams based on such systems. Some characteristics of these ‘third generation’ blowing agents are shown in Tables 4.10, 4.11 and 4.12. These recent developments, which have included foaming trials, have focused attention on the possibilities afforded by HFC-365mfc, and Solvay took a decision to develop

Table 4.9 Comparative costs of rigid PU foam Blowing agent

Comparative cost (%) of 1 m3 of foam to meet DIN EN 1363-2 [10]

DIN EN 1363-1 [11]

HCFC-141b

100

107

CO2 - water

111

114

n-Pentane

96

126

Data from [9]. Reproduced with permission of Rapra Technology

69

characteristics of HFC blowing agents

Handbook of Polymer Foams

Table 4.10 Main characteristics of HFC blowing agents Property

HFC-245fa

HFC-365mfc

Boiling point (°C)

15.3

40.2

Vapour pressure (MPa at 20 °C)

0.124

0.047

Vapour thermal conductivity at 25 °C (mW/m.K)

12.2

10.6

Flash point

none

none

Flame limits (% by volume)

none

3.5-9.0

GWP relative to CO2 = 1

820

840

GWP: Global warming potential Reproduced with permission from [12]. Copyright Rapra Technology, 1999

Table 4.11 Main characteristics of HFC-365mfc/HFC-245fa blends Blend ratio

50/50

95/5

93/7

24

37

20

Flash point

none

none

none

Vapour thermal conductivity at 25 °C (mW/m.K)

11.4

10.7

10.8

Boiling point (°C)

Reproduced with permission from [12]. Copyright Rapra Technology, 1999

Table 4.12 Main characteristics of HFC-365 mfc/pentane azeotropes Pentane isomer

cyclopentane

isopentane

n-pentane

HFC/pentane ratio

73/27

46/54

58/42

Boiling point (°C)

32

22.5

27

Flash point

yes

yes

yes

11.1

13

13

Vapour thermal conductivity at 25 °C (mW/m.K) (calculated)

Reproduced with permission from [12]. Copyright Rapra Technology, 1999

70

Rigid Polyurethane Foams production at pilot scale level with a view to making this substance available as an HCFC-141b substitute [12]. The scenario for blowing agents over the next few years is likely to be: The replacement of polycyclic polyisocyanates -141b in the USA by HFC-365mfc, or a blend thereof; The continued domination in Europe of pentane technology, as it meets Protocol requirements and the safety problems involved with production operations have been solved. In Asia, a mixture of technologies, with some countries (such as China and Korea) still relying on CFC-11. Money is being made available by the World Bank and the United Nations Development Program to subsidise the considerable capital costs involved in changing to flammable blowing agents. Whilst some manufacturers in the Pacific region have made the (relatively easy) change to HCFC-141b, most are now looking at pentane technology to comply with the Protocol and to achieve cost reductions which are important in view of the economic turmoil in Asia. In Japan, conversion to pentane technology is well advanced.

4.2.4 Other Additives

4.2.4.1 Catalysts Foam catalysts have a very substantial influence on process rheology, process latitude, dimensional stability and physical properties. They comprise: •

Tin compounds, e.g.,

Stannous 2-ethylhexanoate Di-butyl tin di-laurate

•

Tertiary amines, e.g.,

Polycat 5 (pentamethyldiethylene triamine) Polycat 8 (dimethylcyclohexylamine) Polycat 41 (tris-dimethylaminopropyl hexahydrotriazine)

•

Quaternary ammonium salts, e.g., Dabco TMR series

•

Potassium salts, e.g.,

Dabco K-15 (Potassium octoate) Polycat 46 (Potassium acetate)

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Handbook of Polymer Foams Tin catalysts mainly promote the reaction between isocyanate and hydroxyl groups, whilst tertiary amines promote both this and the water - isocyanate reaction. Potassium salts catalyse the trimerisation of isocyanates to form isocyanurates. A comprehensive list of catalysts is given in reference [13]. The main technical development in rigid PU foams has been the move away from CFC blowing agents, but there has been substantial formulation development to support this, and to mitigate property changes resulting from use of CFC alternatives. The main suppliers have produced new catalysts which minimise the problems of such formulation changes [14].

4.2.4.2 Surfactants By reducing the surface tension of the polyol, surfactants can perform several useful functions in foam manufacture. They can stabilise the initial liquid-air dispersion (controlling the number of cells); they can emulsify and stabilise a blend of incompatible reagents; and they can stabilise the rising foam. Appliance foam generally incorporates highly functional polyols and isocyanates which results in a relatively high liquid phase viscosity and good foam stability. The surfactant is used mainly to control cell size and to enable blend miscibility of incompatible reagents. Surfactants commonly used, e.g., Dabco DC5357, are copolymers of polydimethyl siloxane and polyalkylene oxide. In all rigid polyurethane foams the change to pentane blowing agents to replace CFC has required surfactant development to overcome the poor solubility of pentane in the polyol (resulting in high viscosities) and a generally higher foam density with a coarser cell structure. Recently developed surfactants, e.g., Nitroil’s PC STAB EP 26+, are claimed to overcome these problems, combining the properties of a foam stabiliser and pentane compatibiliser.

4.2.4.3 Cell Openers The normal open cell ratio in rigid polyurethane foams is 10-20% and for the main application of thermal insulation it is advantageous to retain the blowing agent in closed cells to maintain a low thermal conductivity. In contrast to flexible polyurethane foams, cell opening at the end of the reaction is not required to prevent shrinkage. However, where insulation performance is not the prime concern, cell openers are sometimes recommended to improve dimensional stability. Whereas cell opening of flexible foams can be achieved by mechanical crushing, with rigid foams this would result in permanent compressive deformation. Hence, a chemical method is necessary.

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Rigid Polyurethane Foams A cell opener for rigid foams, Dabco DC5000, has been described [15]. It is designed as a separate additive for use with traditional silicone-polyether surfactants to allow good formulation flexibility. The additive is incorporated in small amounts up to 0.25 parts per hundred (pph) polyol to promote cell window rupture immediately prior to the rapid viscosity build up as the polymeric crosslinked network is formed. It acts by replacing the foam-producing surface film with an alternative film with little or no surface elasticity which rapidly thins and breaks as the foam expands.

4.2.4.4 Blend Compatiblisers One of the major limitations of hydrocarbons as blowing agents is their poor solubility in polyol. Use of higher amounts is desirable, particularly in PIR applications, as it would allow an improvement in reaction kinetics by the reduction or elimination of water. Higher levels of hydrocarbon above the solubility limits can result in phase separation during and before the foam reaction leading to foam inhomogeneity. Goldschmidt, for example, have developed Ortegol 410 which helps to solubilise pentane in rigid foam polyols. Using technical cyclopentane (70% cyclopentane plus mainly n and i isomers) in a European appliance polyol system, clarity up to 11 pph pentane is achieved without additive; with 5.0 pph of Ortegol 410, clarity was maintained up to 15 pph; at 10 pph Ortegol 410, clarity was maintained up to 18 pph pentane [16].

4.2.4.5 Glass Fibre There are few examples of the use of non-reactive fillers in rigid polyurethane foams, but glass fibre is one that was originally developed by Celotex Corporation. Incorporation in PIR foams was found to give additional stability to the protective char formed in a fire situation, hence improving fire performance to meet the USA requirements for built up roofs. An additional benefit is a lower thermal expansion coefficient which leads to improved durability and helps to prevent cracking when hot bitumen is poured onto laminate panels for roofing.

4.3 Manufacturing Processes for Rigid Polyurethane Foam The original method for production of rigid PU foam was simply to pour the foam mix into a box mould. The product was subsequently cut to form boards, pipe shells and other complex shapes. This method is essentially that now used for ‘pour in place’ applications such as insulative linings for refrigerators and similar appliances. Increasing

73

Handbook of Polymer Foams volumes required more economic production methods, and a continuous process for block foam was developed, followed later by continuous lamination technology for panel production. The latter allows efficient production of rigid PU board with different facing materials like bituminous paper, glass fibre reinforced bitumen sheets, multi layer papers or metal sheets. Currently, both discontinuous and continuous processes operate for production of laminated rigid PU panels, although the continuous process (introduced in the late 1960s) is dominant. In a typical continuous process (CONTIMAT), galvanised steel sheets (0.50.8 mm) are wound off large coils and fed through a profiling unit to provide edge and surface profiles. Lower and upper facings pass through simultaneously and are then preheated to the process temperature required. The reactive PU mix is dispensed onto the lower facing using a linear application method whereby the mix head oscillates across the entire plate width. Sophisticated control ensures uniform distribution giving expansion only in the vertical direction, resulting in uniform density through the sheet and optimum production output. An adjustable gap between upper and lower conveyors controls panel thickness. Conveyor lengths are typically 20 to 30 m. Panels are cut to length some 10 m after leaving the conveyor. Output rates of a double conveyor plant with a 30 m length pressure zone and 1.2 m width are typically 860 m2/h (50 mm thickness) and 390 m2/h (150 mm thickness) [17]. Output rate is directly dependent on conveyor length, being 30% lower for a length of 20 m. The discontinuous process comprises a series of steps linked to provide a manufacturing operation. These steps are: •

Preparation and positioning of metal sheets, either from a coil of metal or by use of stacked sheets.

•

Profiling the edge and surfaces of the sheets.

•

Feeding the sheets to a multiple daylight press characterised by a central pressing plate.

The pressing plate moves so as to close an upper mould in preparation for dispensing the PU foam mix whilst releasing the lower mould for removal of the finished panel and insertion of further facing sheets. Such presses may be configured, e.g., as 1+1, 2+2, 3+3 or 4+4. Optimum output of a discontinuous process is achieved when curing time and operating time are of equal duration and when the platen area of the presses is fully utilised. Typical output rate of a 4+4 daylight press, 6 m long, 1.2 m wide, maximum platen area utilised, is 150 -170 m2/h (50 mm thickness) and 40 -50 m2/h (150 mm thickness) [17].

74

Rigid Polyurethane Foams A joint cooperation between Hennecke GmbH and Bayer AG has resulted in the VarioCast process which is claimed to not only reduce the cycle time for discontinuous panel foaming operations but also to improve cell structure, increase dimensional stability and reduce raw material costs by 5%. The equipment is modular, is said to give cycle time savings up to 30% and is compatible with various blowing agents including pentane. The continuous process has higher output rates and there is no technical limitation on panel length (in Europe, currently up to 18 m). Foam densities are generally lower than those of foam produced by the discontinuous process (40-45 kg/m3 versus 45-55 kg/m3). In the discontinuous process, panel length is limited by press dimensions, but there is greater flexibility in the use of facing materials (these may include chipboard, plywood, or light building board, in addition to the usual steel or aluminium sheet). Cell structure and uniformity is inferior in the discontinuous process since the distribution of reaction mixture is non uniform and expansion occurs sideways as well as vertically. Dimensional stability of the foam is adequate but inferior to that from the continuous process. There is, however, more scope for sheet profiling, including ends as well as sides, which is not feasible in the continuous system. It is also possible to spray foam in place for insulative or sealing applications. Formulations are required with high reactivity and low odour. Considerable development has been carried out on rigid polyurethane foam processes in recent years to overcome the problems imposed by the change from CFC blowing agents to hydrocarbons. The main problem is the flammable nature of hydrocarbon blowing agents which requires special precautions to enclose the process to ensure there is no chance of any vapours escaping, and removing any possible source of ignition. The necessary technology is now well developed and equipment capable of handling these substances is now available from all the main manufacturers.

4.4 Recycling Processes for Rigid Polyurethane Foam Whilst rigid PU foam is a stable product with a long lifetime, material for disposal can arise when, for example, appliances are scrapped or when underground insulated pipes are replaced. It naturally arises also from within a process from trimming and from out of specification foam during start-up and change-over. Companies are giving increasing attention to the problems of waste due to environmental concern and the cost of disposal. Many companies use glycolysis to process their relatively pure PU scrap whilst other wastes are dealt with by a mechanical process. Glycolysis turns the PU waste back into polyols for new rigid PU slabstock production and is a process which has been used for many years.

75

Handbook of Polymer Foams In a recycling method developed by Puren Schaumstoffe [18], PU waste is mixed with scrap PET from, for example, soft drink bottles. This has the advantage of reducing methylene diphenylamine levels arising from MDI based PU which can reach undesirable levels if only PU waste is used. Contaminated waste, i.e., waste containing PU foam mixed with covering paper, mineral wool, glass wool, aluminium sheet, etc., is first separated and pressed into briquettes which are then granulated and transported to a mixing system. An MDI-based binder is added and the mixture pressed at 140-160 °C at a pressure of 1-3 MPa for about 3060 seconds to form boards which are subsequently cut to size. The product is said to have good mechanical properties, low heat conduction and is moisture resistant. Thicknesses range from 5 to 60 mm and densities from 250 to 850 kg/m3. Various construction applications are envisaged, including floor insulation and sandwich elements. The process was sufficiently successful for Puren to decide in 1997 to build a second plant to increase capacity. BASF have developed a ‘second generation chemistry’ using glycolysis to recover polyols from a variety of PU systems including rigid PU foam. Residual amine is claimed to be less than 1%. The polyols are said to be reusable in polyisocyanurate foam, insulation non-critical foam, structural foam, friable energy absorbing foam, low density void filling foam, elastomeric coatings, rigid non-cellular PU, and moulded semi-rigid foam.

4.5 Properties of Rigid Polyurethane Foams Some of the properties of rigid PU foam important in its applications are: •

High insulating capacity with low thickness

•

Lightweight, with high mechanical strength

•

Chemically and biologically resistant

•

Durable

•

Satisfies fire regulations for particular applications

•

Quickly and easily processed on site. Can be sprayed in place.

Physical properties of a continuously produced pentane blown PIR (insulating panel) are shown in Table 4.13.

76

properties of Pentane blown PIR foam Rigid Polyurethane Foams

Table 4.13 Properties of pentane blown PIR foam Property

Value

Density (kg/m3)

32

Compressive strength (MPa) - perpendicular

0.22

Compressive strength (MPa) - in belt direction

0.12

Compressive strength (MPa) - across belt

0.13

Flexural strength (MPa)

0.42

Brittleness (%)

25

DIN EN 1363-1 [11] (cm)

12

Closed cell count (%)

98

Dimensional stability (70 °C/95% RH) (%)

+1.04

Thermal conductivity (mW/m.K) - initial

19.9

Thermal conductivity (mW/m.K) - after 3 months at 70 °C

23.9

Reproduced with permission from [19]. Copyright 1999, Carl Hanser Verlag

In many applications, insulation is the characteristic of most importance, and considerable work has been done to investigate the performance of rigid foams with the newer blowing agents, in particular their long-term performance. Predicting long-term performance from short-term accelerated ageing tests has also received recent attention. Some published data are shown in Table 4.14. Analysis of gas in the cells showed the loss of blowing agent and its replacement by air associated with the deterioration in insulation performance. Thicker foams show a slower loss, as expected. The loss at 70 °C after 39 weeks, whilst substantial, was still less than the value after 5 years at 23 °C. Ball has described a method for predicting long-term (25 years) ageing values based on measuring the increase in thermal conductivity after 25 weeks at 70 °C [7]. It is claimed the method is satisfactory irrespective of rate of ageing and the presence of facings. This work indicates that HCFC-141b and n-pentane blowing agents are similar to CFC-11 and CFC-12 in that a stable thermal conductivity value is reached in less than 25 years,

77

thermal conductivity of Rigid PU foam boards Handbook of Polymer Foams

Table 4.14 Thermal conductivity of rigid PU foam boards after ageing Blowing agent

Product thickness

Thermal conductivity at 10 °C (W/m.K) after ageing at 23 °C or 70 °C 6 weeks

2 years

5 years

at 23 °C

25 weeks

39 weeks

at 70 °C

Pentane

40 mm

0.0237

0.0267

0.0272

0.0266

0.0266

Pentane

80 mm

0.0230

0.0252

0.0263

0.0255

0.0257

HCFC-141b

50 mm

0.0203

0.0243

0.0252

0.0229

0.0231

HCFC-141b

60 mm

0.0192

0.0247

0.0257

0.0229

0.0231

Data used [20] with permission from Rapra Technology

and this value is likely to be maintained well beyond 50 years. the predictive formulae given by Ball for 25 year values (Æ25) are : CFC blown

Æ25 = (Æ1 - 6.5) mW / m.K

Pentane blown

Æ25 = (Æ1 - 5.4) mW / m.K

HCFC-141b blown

Æ25 = (Æ1 - 6.7) mW / m.K

where Æ1 is the initial value (measured after less than two days ageing for thin samples).

4.6 Applications The two major applications for rigid PU foam are in construction and in appliances such as household refrigerator liners.

4.6.1 Applications in Construction In the construction industry, rigid PU foam is used both as insulating boards and panels, and as an in situ material for sprayed-in-place insulation and as a one component bonding foam. Boards are used in pitched and flat roofs, in suspended ceilings, in floor slabs with or without underfloor heating, in walls for external, internal or cavity insulation (with rendering if required) and in a wide range of buildings from multi-storey car parks to

78

Rigid Polyurethane Foams farms. Load bearing rigid sandwich panels formed by combining the rigid PU foam with rigid wood or metal sheet facings are used for insulating roof and wall cladding. In thicknesses greater than 100 mm, PU sandwich panels are used for cold storage facilities and for refrigerated storage and transport. Roofs and industrial components such as tanks or pipes may be insulated by using polyurethane spray to produce an insitu foam. Doors and window frames can be fixed and joints sealed using one component bonding foams. In roof, wall, floor and ceiling applications, rigid PU foam has much in common with polystyrene foam which is used for similar insulation applications. The insulation market, however, is dominated by mineral or glass fibre wool which, whilst less technically attractive, costs less as a material and more easily meets fire resistance requirements. Some data given by Kaufung, Bayer AG, on the market share of various materials for insulation applications [21] are shown in Table 4.15.

Table 4.15 Insulation material - Western Europe market (1995) Volume (106 m3)

Share (%)

Mineral wool/glass fibre wool

52.6

60.5

Phenolic foam

0.9

1.0

Rigid PU foam

6.4

7.4

Expanded polystyrene foam

24.1

27.7

Extruded polystyrene foam

3.0

3.4

Total

87

100

Material

Data from [21]. Copyright SPI, 1997

The demand in construction has been growing and this growth is expected to continue at a rate greater than that of the construction industry itself, in line with increasing demands for the improved comfort provided by insulation, and the energy savings available when insulation is used. Environmental as well as economic pressures are driving this. Weigand [22] has examined the environmental benefits of rigid PU insulation by carrying out an ‘eco-balance’ calculation for pitched roof insulation and floor insulation. Savings in energy used for heating during use far outweigh the environmental ‘costs’ of production and eventual recovery. The positive environmental effect of using an appropriate level of insulation has also been shown by Ashford [23].

79

Handbook of Polymer Foams

4.6.2 Applications in the Appliance Industry The use of rigid PU foam for refrigerator insulation is the other main application for the material. In 1997, the consumption of PU worldwide in refrigerators was 464 tonnes, some 40% of the amount used in construction. A breakdown given by Bayer [24] is shown in Table 4.16.

Table 4.16 Shipments and PU consumption of refrigerators and freezers in main world regions (1997) Region

Shipment (millions of units)

PU consumption (k tonnes)

Share (%)

Europe

18.9

155

33

USA

11.5

98

21

Japan

4.8

28

6

South America and Mexico

10.7

54

12

China

13.2

78

17

Far East and India

12.0

51

11

World Total

71.1

464

100

Data from [24]

The larger markets in Europe, North America and Japan are well developed [24] and although there is a trend towards larger and more sophisticated appliance models to meet customer demand, the growth of the market in these countries is small or nil. Worldwide, these countries account for 60% of the total. The market in less developed countries however, is not yet saturated and still shows significant growth. Between 1993 and 1995, European refrigerator manufacturers moved away from CFC blowing agents, mostly to cyclopentane, although HCFC-141b, HCFC-141b/HCFC-22 blend, and hydrocarbon blends have also been used. In the USA, as with rigid PU foams for construction, HCFC-141b was the preferred blowing agent. In Europe, whilst initially the resulting poorer performance of the non-CFC foams was accepted (higher density and hence higher shot weight, lower insulation value), subsequent development work has aimed to meet the overall properties of the original CFC foams.

80

Rigid Polyurethane Foams Legislation has been one of the driving forces, involving not only the Montreal Protocol, but also regulations on the reduction of appliance energy consumption introduced by the EU, and the voluntary Eco-Label of the EU. The key requirements for the Eco-Label are: •

Sufficient insulation for the refrigerator to be rated A or B according to the 94/2/EC Energy Efficiency Index regulation. For an A rating, energy consumption must be below 55% of the standard value defined by the EU directive, whilst for a B rating energy consumption must be between 55 and 75% of this value.

•

Foam blowing agent must have an ODP of zero and a GWP of no more than 15 CO2 equivalents.

The blowing agent requirements rule out both HCFC and HFC, limiting candidates to hydrocarbons or carbon dioxide. The appliance energy consumption regulations and the Eco-Label arrangements came into force in 1999 (96/57/EC). In the USA, HCFC-141b use is allowed by the US Environmental Protection Agency (EPA) as a transition measure until energy efficient, zero ODP, replacements become available. Formulation development has enabled such foams essentially to match the insulation performance of the CFC foams they replace, enabling refrigerator and freezer manufacturers to remain in compliance with US Department of Energy (DOE) consumption regulations. The deadline for replacing HCFC-141b in the USA was set by the US EPA as 1st January 2003. Additionally, the US DOE issued an energy consumption regulation for refrigerators and freezers sold from July 1st 2001. This calls for up to 30% reduction in energy consumption from the levels permitted under the 1993 regulations. The US DOE has estimated that this will result in significant savings in primary energy consumption and a consequent reduction in carbon dioxide emissions amounting to some 465 million tonnes over 30 years. In Japan, there are no regulations for energy consumption for appliances although the importance of energy saving is well recognised in the industry and strongly supported by the government. The saturation of the market in Japan is illustrated by the figure of 1.2 refrigerators, on average, for each Japanese household. The growth regions of South America and South-East Asia are less advanced in both CFC replacement and energy reduction regulations, but the technologies now available are being put in place and Brazil, for instance, has a regulation to eliminate CFC in household refrigerators which came into force on January lst 2001.

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Handbook of Polymer Foams China and India are areas where the relatively low market saturation offers good market growth potential. The change over from CFC is happening - albeit slowly as use of CFC is still permitted under the Montreal Protocol - the trend being initially to the ‘drop-in’ HCFC systems with hydrocarbons being used in some joint venture foam plants involving European companies. Development trends in the industrial countries are targeted on cost reduction whilst continuing to meet environmental legislation for blowing agents and energy consumption. In Europe and Japan, this focuses on improving hydrocarbon blown foams either by improving existing pentane-based systems or by development of systems based on cyclopentane blends with various butane and/or pentane isomers. The latest systems are claimed to match the properties of CFC-11 foams [24], having lower cabinet fill weights, shorter demould times and improved insulation factors. This has been achieved by tailoring the basic polyol and isocyanate materials to the requirements of the new blowing agents formulated for use with CFC. In the USA, HFC-245fa has been identified as the most suitable replacement for HFC141b in appliances. Work done by ARC and Bayer has shown that appliance insulation made using this blowing agent has an energy consumption matching that of HCFC-141b systems. Vacuum insulation panels are also receiving attention as this technology is able to provide improved k factors (a measure of insulation). However, manufacturing and installation costs are high and only a few manufacturers in USA, Europe and Japan offer appliances with such insulation. This may change with further tightening of energy consumption regulations. It can be expected that development will continue so as to satisfy customer and legislative requirements, and it will be some time before formulations world wide focus on one or a few systems recognised as economically and environmentally optimal.

References 1.

C.J. Benning, Plastic Foams: the Physics and Chemistry of Product Performance and Process Technology, Wiley-Interscience, New York, NY, USA, 1969.

2.

Polyurethane Technology, Ed., P.F. Bruins, Interscience, New York, NY, USA, 1969.

3.

D. Reed, Urethanes Technology, 1999, 16, 1, 32.

4.

R. Brooks, Urethanes Technology, 1999, 16, 1, 34.

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Rigid Polyurethane Foams 5.

Dow Polyurethanes - Flexible Foams, 2nd Edition, Ed., R. Herrington, Dow Chemical Company, Midland, MI, USA, 1997.

6.

UNEP web site, www.unepie.org

7.

G.W. Ball, A. Simpson and H. Fleming, Cellular Polymers, 1997, 16, 2, 110.

8.

A. Cunningham, I.D. Rosbotham, and A.K. Thomas in Proceedings of the SPI 32nd Annual Conference, Polyurethanes ‘89, San Francisco, CA, USA, 1989, p.522.

9.

L. Bertucelli, M. Vreys, F. Pignagnoli, A. Ottens and P. Keller, Proceedings of Utech Asia ‘99, Suntec City, Singapore, 1999, Building and Construction, Paper No.6.

10. DIN EN 1363-2, Fire Resistance Tests - Part 2: Alternative And Additional Procedures, 1977. 11. DIN EN 1363-3, Fire Resistance Tests - Part 1: General Requirements, 1999. 12. L. Zipfel, P. Dournal and W. Kruecke in Proceedings of Utech Asia ‘99, Suntec City, Singapore, 1999, Building and Construction, Paper No.7. 13. K. Ashida and K. Iwasaki in Handbook of Plastic Foams: Types, Properties, Manufacturers and Applications, Ed., A.H. Landrock, Noyes Publications, Park Ridge, PA, USA, 1995, Chapter 2, p.30-38. 14. D.E. Eaves, Polymer Foams, Trends in Use and Technology, Rapra Technology, Shawbury, Shrewsbury, UK, 2001. 15. K.F. Mansfield, J.W. Miller and W. Wong, Proceedings of Utech Asia ‘99, Suntec City, Singapore, 1999, Appliance, Paper No.5. 16. G. Burkhart and M. Klincke in Proceedings of Utech Asia ‘97, Suntec City, Singapore, 1997, Paper No.27. 17. D. Chua, Proceedings of Utech Asia ‘99, Suntec City, Singapore, Building and Construction, Paper No.4. 18. M. Knoedgen, Urethanes Technology, 1998, 15, 6, 34. 19. H. Schmidt and E. Calgua, Kunstoffe Plast Europe, 1999, 89, 2, 36. 20. W. Albrecht and H. Zehendner, Cellular Polymers, 1997, 16, 1, 35.

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Handbook of Polymer Foams 21. R. Kaufung in Proceedings of the SPI Polyurethanes ’97 World Congress, 1997, Amsterdam, The Netherlands, p.2. 22. E. Weigand, Insulation Journal, 1999, March/April, 11. 23. P. Ashford in Proceedings of SPI Polyurethanes World Congress ‘97, Amsterdam, The Netherlands, p.612. 24. Urethanes Technology, 1997, 14, 4, 42.

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5

Flexible Polyurethane Foam Tyler Housel

5.1 Introduction Polymer foams that are made primarily from polyol, isocyanate and water are known as flexible polyurethane foams (FPF). In this chapter, we will discuss both slabstock and moulded FPF with a density of less than about 100 kg/m3. The goal is to provide a general introduction to the chemistry, manufacturing, testing, and commercial aspects of FPF. Rigid polyurethane foams are covered elsewhere in this book. Readers are encouraged to use the citations to obtain more detailed information in areas of particular interest. The earliest work on FPF was published in Germany in the 1940s [1]. A viable commercial process was quickly developed, and within a decade there were manufacturing sites in both Europe and North America. By the year 2000, more than three million tonnes of FPF were produced around the globe [2]. The industry continues to grow and expand into new markets, and foam grades are constantly being developed and improved to meet the ever-increasing demands of the end users.

5.2 Chemistry The solid polymer that makes up the struts and membranes of an FPF is called polyurethane by convention, but is really much more than that. It is a polymer with ester and/or ether bonds from the polyol portion, and urethane and urea bonds from the reactions of isocyanate. Polyurethane foam starts out as a liquid mixture of three reactants with a number of additives. Within a few minutes it becomes a solid network of polymer that can have 99% of its volume filled by air. Despite the complexity of the system, the chemistry used to describe it is actually quite simple. Isocyanates are involved in all of the chemistry that occurs during polyurethane foam manufacturing. The two major reactions are known as the ‘gel’ and ‘blow’ reactions. The gel reaction takes place between isocyanate and hydroxyl groups to yield a urethane linkage that builds molecular weight and gels the polymer. The blow reaction occurs in

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Handbook of Polymer Foams two steps and consumes one water molecule and two isocyanate groups. Water first reacts with isocyanate to produce a carbamic acid intermediate that quickly decomposes to give an amine and carbon dioxide. Carbon dioxide is the blowing gas which fills the cells. The amine reacts with a second isocyanate to form a urea linkage. Both the gel and blow reactions build molecular weight and therefore cause the polymer to gel, but the blowing gas is only produced from the water reaction. These reactions are shown in Figures 5.1 and 5.2.

Figure 5.1 Gel reaction

a)

b)

c)

Figure 5.2 a) Blow reaction - first stage; b) blow reaction - decomposition step; c) blow reaction - urea formation

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Flexible Polyurethane Foam For completeness, it must be mentioned that isocyanate will react with any active hydrogen compound, including the urethane or urea group formed earlier. It will also react with itself to form dimers and trimers [3]. These crosslinking reactions occur to varying degrees in all foam systems but are generally slower than the gel and blow reactions. Rather than consider each individually, the isocyanate index allows the formulator to account for the minor reactions as a group. The isocyanate index is the percentage of isocyanate groups relative to the total active hydrogen groups from water and hydroxyl in the formula. Remember, each water molecule reacts with two isocyanates so the following formula must be used: Isocyanate index =

equivalents isocyanate x 100 _ equivalents hydroxyl + 2 x equivalents water

An index of 100 means that there are exactly enough isocyanate groups to completely consume the water and hydroxyl groups in the formula. This means that a foam with an index of 110 was made with 10% extra isocyanate. There is no active isocyanate in a cured block of foam [4], so the extra isocyanate must be consumed by the various side reactions. Increasing the isocyanate index makes the foam stiffer, presumably because the extra isocyanate reactions increase crosslinking in the polymer matrix. Most FPF has an index between 90 and 110 although there are special grades outside that range. While the chemistry is easy to describe, it becomes more complicated when considering the number of possible permutations. In most foam systems the reactive groups include three types of active hydrogen (primary hydroxyl, secondary hydroxyl and water) and two types of isocyanate (hindered and unhindered). Even ignoring the minor reactions, this gives six possible reactions that can occur, and each has a different sensitivity to catalyst and temperature. Beyond that, the ingredients are not mutually soluble so some groups may be more available to the isocyanate than others [5]. All of this also changes with time as polymer is formed [6]. A skilled formulator knows how different variables will affect the final product, but inevitably, some trial and error is used to optimise the formula.

5.3 Starting Materials There are five ingredients that are common to all flexible polyurethane foams: isocyanate, polyol, water, catalyst, and surfactant. However, few formulations are actually that simple. There are a number of other additives that can be used to improve processing, performance, appearance, or stability of the foam. By choosing the raw materials and process conditions

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Handbook of Polymer Foams carefully, the manufacturer controls the physical properties, mechanical properties and appearance of the foam [7].

5.3.1 Isocyanate As previously mentioned, all of the reactive chemistry that occurs during the foam manufacturing process involves isocyanate groups. Several isocyanates are commercially used in the polyurethane industry, but the majority of slabstock foams (those made in long, continuous blocks) are made with toluene diisocyanate (TDI) (see Figure 5.3). This is a low viscosity aromatic isocyanate that has hindered and unhindered isocyanate groups that react at different rates. The most common grade is known as TDI-80, which has an 80/20 mole ratio of the 2,4 and 2,6 isomers of TDI. TDI-65 is also popular in Europe, but infrequently used in the rest of the world. With its higher content of the 2,6 isomer, TDI-65 gives a stiffer foam with a more open cell structure.

Figure 5.3 Isomers of TDI Isocyanates derived from methylene diphenyl diisocyanate (MDI) are used in both moulded (those made in a closed mould) and slabstock [8] foams. These are also preferred for low resilience viscoelastic foams [9]. MDI types cover a number of related chemical structures. Pure MDI is not often used in flexible foams because it is a solid that must be used in its molten form. Foam grade liquid MDI derivatives can be unpurified intermediates from the pure MDI process or can be chemically modified to impart desired properties. Besides TDI and MDI types, aliphatic isocyanates are used in a few highly specialised formulas where light stability is an absolute necessity.

5.3.2 Polyol In the polyurethane industry, the term polyol describes any oligomer with two or more active hydroxyl groups that react with isocyanates during the foaming process. Flexible

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Flexible Polyurethane Foam foams are normally made with polyols that have molecular weights from several hundred to several thousand and hydroxyl functionalities from two to three. The polyol gives flexibility to the polymer, so lower molecular weight and/or higher functionality polyols will produce a stiffer foam. In the foam industry, three major types of polyol are prevalent, and each has its own advantages as shown in Table 5.1. The greater use is from polyether polyols. Most of these start with a trifunctional initiator such as glycerine. Ethylene and propylene oxides then react with the initiator to give polyether chains terminated with hydroxyl groups. Moulded foams often work better with more reactive polyols, so ether polyols for moulded foams are terminated with ethylene oxide (EO) to give more reactive primary hydroxyl groups on the ends. These ‘EO capped’ polyethers are less commonly used in slabstock foams. Polyester polyols are made from diacids and diols that react to give polymer chains with repeating ester bonds. Essentially all polyester slabstock polyols are made from diethylene glycol (DEG) and adipic acid. Glycerine or trimethyl propane (TMP) are added to the charge to increase the hydroxyl functionality to the 2.5 to 3.0 range. Flexible moulded polyester foams are made from adipates of short chain glycols such as DEG, ethylene glycol and butanediol. If higher functionality is required, small amounts of TMP are reacted into the polyol. Moulded foams are more prone to shrinkage, so these polyester polyols rarely have functionalities above 2.5. Copolymer polyols are normally derived from polyether polyols. They are sometimes called polymer, graft or filled polyols [10] (note: some sources use the term ‘filled’ to refer to polyols filled with mineral fillers only, excluding the copolymer polyols [11]). These are primarily used to increase strength, hardness and resilience. One type of polymer polyol uses a free radical initiator to polymerise unsaturated monomers such as styrene and acrylonitrile (SAN polyols) that are added to a polyether polyol. The free radical

Table 5.1 Foam polyol property summary Property

Polyether polyol

Polyester polyol

Copolymer polyol

Viscosity

low

high

medium

Hydrolytic stability

excellent

fair

excellent

Oil/solvent stability

fair

excellent

good

Strength

fair

excellent

very good

good

fair

excellent

Resilience

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Handbook of Polymer Foams will occasionally react with the polyether chain, grafting the polymer to the polyol. The other main type of polymer polyols are the PHD polyols. The name comes from ‘PolyHarnstoff Dispersion’ which is German for polyurea. These are made by adding amines and isocyanates to a polyol. The isocyanate will react much more quickly with the amine, so they are essentially dispersions of polyurea in polyol. Either of these techniques gives the polyol a milky appearance and causes a significant increase in viscosity. Most copolymer polyols are based on low viscosity polyethers despite the excellent properties of copolymer polyester polyols [12].

5.3.3 Water Water reacts with isocyanate to produce the carbon dioxide (CO2) that eventually fills the cells and foams the polymer. Flexible foams normally use between 1 and 6 parts of water, with higher water levels leading to a lower density foam. The water-isocyanate reaction is extremely exothermic, so low density water blown foams are prone to thermal discoloration in the centre of the bun where the temperature is hottest for the longest time. In extreme cases, it becomes dangerous to produce very low density water blown foams as they can self ignite. For this reason, most foams below 15 kg/m3 are blown with a combination of water and a non-reactive blowing agent. Variable pressure foaming (VPF) is another way to produce low density foams with moderate water levels.

5.3.4 Surfactant Surfactants (or stabilisers) are essential, multifunctional additives that make polyurethane foam possible. These are often a combination of ingredients that serve three purposes during the foaming process. The first role of the surfactant is to lower the surface tension of the liquid in the mix head so that bubble nuclei can form from the available energy [13]. These nuclei determine the size and structure of the cells in the foam. The second role is to emulsify the water, polyol, isocyanate and additives. If the dissimilar liquid components do not emulsify properly, large scale deformities are produced in the final foam. As the foam rises, cell membranes form between gas bubbles, and the surfactant is also responsible for stabilising these membranes. Yet the surfactant must also allow the thinned membranes to rupture during the cell opening phase. This balance of stability and instability is the key to developing a successful foam formulation. There are many types of foam surfactants and each is usually specific to the type of formulation being poured. For example, surfactants designed for polyester foams will not work in polyether systems and vice versa. Within each category, different surfactants are available depending on the density, porosity, cell structure and other properties desired.

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Flexible Polyurethane Foam Most have a combination of emulsifying, stabilising and destabilising ingredients that are engineered to work together. While it is possible to meter the individual components to the mix head as separate streams, this is rarely done in practice because the surfactant supplier blends them in the appropriate ratio.

5.3.5 Catalyst Most FPF systems reach full rise in less than two minutes, and parts or slabs are handled only a few minutes after that. Not only does a fast reaction improve manufacturing efficiency, it also minimises the critical time between cell opening and strength development that determines whether the product is good. Foams with longer reaction times are more likely to have a poor cell structure and problems with shrinking, settling or collapse. Isocyanates react sluggishly with water and alcohols at room temperature, so catalysts are added to accelerate and control the rise and cure of moulded and slabstock foams. There are several competing chemical reactions that take place during the foaming process, and every catalyst affects each reaction differently. Nothing is completely selective, but gel catalysts primarily speed the reaction between polyol and isocyanate, and blow catalysts are more selective to the reaction between isocyanate and water that generates the blowing gas. A balanced catalyst has similar activity for both reactions. It is important to remember that the type of polyol strongly affects the catalyst requirement. Polyether polyols with a high percentage of secondary hydroxyl groups require much stronger gel catalysts than EO capped or polyester polyols. Catalysts also show varying degrees of activity toward the different side reactions such as allophanate, biuret, and isocyanurate. In rigid foams, these can be critical, but in flexible systems the side reactions are normally ignored. Lastly, temperature affects some catalysts more strongly than others. Delayed catalysts are commonly used in moulded foams to give fast demould times without shortening the time to fill the mould. These become active only after the reaction exotherm increases the temperature. Many organometallic compounds are effective gel catalysts, the most common of which are stannous octoate and dibutyl tin dilaurate. Recent toxicity concerns have reduced organotin usage in Europe. Trialkyl amines such as triethylene diamine are also used as gel catalysts although they are less selective than the organotins. Delayed gel catalysts are usually trialkyl amine salts that will unblock at higher temperatures [14]. Blow catalysts are tertiary amines that have two carbons separating the catalytic amine from another tertiary amine or an ether group. This structure is believed to form a complex with water molecules that enhances their reactivity with isocyanate [15]. Bis (N, N,

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Handbook of Polymer Foams dimethylaminoethyl) ether and the structurally similar pentamethyl diethylene triamine are widely used as strong blow catalysts. Morpholine and piperazine structures are generally weaker and more balanced. Successful foaming requires a balance between the gel and blow reactions. It is not possible to make a universal balanced catalyst, but a number of catalysts are available that are balanced for a particular system. These can be a single compound or a blend of gel and blow components. In practice, most manufacturers use a catalyst system that somewhat favours the blow reaction and then add minor amounts of a strong gel catalyst to allow for daily adjustments. This is also useful for manufacturers that make several different grades of foam because they only need a few catalysts to make many types of foam. Reactive catalysts are frequently used to avoid volatile amine emissions. These have reactive hydroxyl groups that enable them to become part of the chemical network. Dimethyl ethanolamine (DMEA) is an inexpensive gel catalyst, while methyl hydroxyethyl piperazine is a weak blowing catalyst. Triethanolamine is commonly used as a catalyst and crosslinker in moulded foams.

5.3.6 Colorants Natural polyurethane foam is an off-white colour that yellows over time with exposure to air and light. Colorants are added to improve the aesthetic appeal, hide the natural yellowing and give an easy way to tell different foam grades apart. Both pigment and dye-based colorants are available for any type of polyurethane foam. These are usually supplied as a concentrated liquid or paste in a low molecular weight polyol carrier. Colorants with polyester carriers can be used for any type of foam, but polyether carriers can cause pinholes in polyester foams. Carbon black is widely used to make different gray and charcoal grades of foam. Most colours can be made by mixing different ratios from a palette of 3-4 primary colours. White or blue-white pigments are sometimes used to make white foam appear brighter and resist yellowing with age.

5.3.7 Antioxidants Antioxidants are added to protect the colour of a slabstock foam during processing. The foaming reactions are extremely exothermic, and the centre of a large block of foam can reach 170 °C [16] and remain hot for many hours. Under these conditions, thermal oxidation can yellow or ‘scorch’ the foam in the centre. Antioxidants can reduce scorch, but if the block remains too hot for too long, any antioxidant will be overwhelmed and scorch will still be visible. Recent work in exotherm management shows that additives

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Flexible Polyurethane Foam can significantly reduce scorch by lowering core temperature by 25 °C [17]. At the very least, it is important to allow space between curing foam blocks so they can cool as quickly as possible.

5.3.8 Light Stabilisers Most antioxidants provide only a slight benefit in keeping the foam from yellowing over time. Light stabilisers are more effective in reducing long-term yellowing, but again they will slow the process but not prevent it. The only sure ways to make non-discolouring foam is to either make it black or to use an aliphatic isocyanate.

5.3.9 Flame Retardants Some of the largest markets for flexible polyurethane foam are for furniture, bedding and automotive parts. In these applications, the foam is required to meet strict flammability specifications that limit the speed and extent of combustion. To meet these requirements, the manufacturer adds flame retardants that inhibit the combustion process [18]. There are several types of flame retardants, and each has its own benefits and drawbacks. Further, all tend to increase density and reduce the durability and mechanical properties of the foam. The most widely used materials are chlorinated phosphate esters such as tris dichloro isopropyl phosphate (TDCP) and tris monochloro isopropyl phosphate (TCPP). These are very effective in many grades of foam, but their health effects have been questioned, and they contribute to foam discolouration (scorching) [19]. Pentabromo diphenyl oxide gives much less scorch and is widely used in North America but is facing a ban in some European countries because its structural similarity to polychlorinated biphenyls may indicate long-term environmental issues [20]. Other brominated materials are now being introduced that should have a more favourable profile [21]. Powdered melamine is synergistic with chlorinated phosphate esters and brominated materials and is frequently used to improve the performance of flame retarded foams, particularly to meet Cal TB 133 [22] and BS 5852, CRIB 5 Test [23] requirements [24]. Melamine has a favourable toxicological and environmental profile, but doesn’t work universally [25]. It requires high amounts of additive that can make the foam difficult to process [26] and can negatively affect mechanical properties [27]. There are other flame retardant chemicals that are used in minor amounts in FPF. These include aluminium trihydrate, ammonium polyphosphate, antimony trioxide, barium sulfate, graphite and tribromo neopentyl glycol.

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5.3.10 Adhesion Promoters Automotive parts are often made of vinyl with a moulded foam filling. Polyester foams have excellent adhesion to vinyl but insufficient flow properties for this application. Polyether foams have good flow but poor adhesion. To overcome the inadequacies of each system, the moulder can use a polyol blend that contains small quantities of ester polyol as an adhesion promoter to a polyether moulded foam. In this way, both flow and bond strength are acceptable. In a similar manner, ester-ether hybrids are sometimes used for slabstock foams designed for textile lamination. These foams are bonded to textiles to give the strength and aesthetic appeal of the fabric with a padded feel. The lamination process involves passing a thin sheet of foam over a flame and quickly pressing the melted foam against the fabric. Polyester foams give a much better bond, but cannot be used for some applications because of their long-term hydrolytic degradation. It has been found that the lamination properties of polyether foams can be significantly improved by adding small quantities of polyester polyols to the formula. It has been proposed that small quantities of acid in the foam favourably affect flame bonding [28].

5.3.11 Other Additives Polyurethane foam is naturally non-conductive, and it can build up static electricity in certain environments. Anti-static additives help static dissipation for foams that are used in the aircraft of electronics industries. Biocides can be added to protect foam from bacterial or fungal attack if the foam is used where microbial growth is likely. Cell modifiers can be used to make the foam coarser or to give the ‘double cell’ appearance of a natural sponge. Plasticisers can be used to make softer foam. Clickability additives allow the fabricator to cut the foam with a razor edge die without pinching the edges. Mineral fillers increase density which can improve sound absorption, but may reduce durability. Melamine and mineral flame retardant additives act as fillers, while phosphate esters and brominated compounds can plasticise the foam.

5.4 The Foaming Process FPF starts as a mixture of liquid chemicals and within a few minutes becomes a matrix of solid polymer with a uniform, flexible, cellular structure. There are five discrete stages to the foaming process: raw material conditioning, mixing, growth, cell opening and cure. Distinctly different chemical and physical changes occur in each stage, and all affect the final product.

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5.4.1 Raw Material Conditioning A polyurethane foam manufacturer controls many of the chemical and mechanical inputs to the process, but once the liquid leaves the mix head, chemistry and physics determine the fate of the foaming mass. The only way to produce consistent foam is to start with consistent raw materials. The ingredients arriving at the mix head must be at the right temperature and should also have a certain amount of dissolved gas. If these properties vary outside the normal range, defects may result. The main reason for controlling temperature is that some chemical reactions are more thermosensitive than others. The temperature affects the overall rate of reaction, and even the relative rates. This can lead to an imbalance that changes the properties of the final product. Viscosity also changes with temperature, and this affects flowability and mixing. Gas molecules dissolve in polyol and isocyanate as it comes in contact with air during transportation and storage. Dissolved gas is essential for cell nucleation in the mix head. If raw materials are too fresh (not enough dissolved gas) insufficient nucleation can result in a cell structure that is too coarse; conversely, old raw materials can make the cells too fine. Most manufacturers age the major ingredients before use, and some even monitor dissolved gas in the raw materials. Manufacturers can use vacuum or pressurised gas [29] to reduce or increase the dissolved gas in the raw materials, particularly TDI [30]. It is important to recognise that dissolved gas in the liquid ingredients is not the same as bubbles which are undissolved gas. Bubbles can form when pumping viscous raw materials such as polyester polyols, or they can come from air in the raw material lines. This can occur when a filter is changed for example. If air bubbles get into the mix head, pinholes and other defects may result. Occasionally air is intentionally added at the mix head to provide additional nucleation sites. This is most common when an irregular cell structure can be beneficial (high resilience foams), or when a large number of nucleating sites must be present as the mixture leaves the chamber (liquid carbon dioxide blown systems) [31].

5.4.2 Mixing The mix head is where the isocyanate is mixed with water, polyol and other ingredients. Often, some raw material streams are blended prior to entering the mixing chamber, but once the isocyanate, polyol and water are together, the chemistry begins. The mix head serves two critical functions: mixing the ingredients and forming the bubble nuclei that will become cells in the foam.

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Handbook of Polymer Foams Since the residence time in the mixing chamber is normally much less than one second, it must be highly efficient to ensure that the liquid leaving is completely homogeneous. After the mixing stops, dissimilar components will naturally begin to phase separate. However, if there are unmixed regions at the outset, they will lead to large scale defects in the foam. Cell nucleation occurs when dissolved air cavitates into tiny bubble seeds. Tremendous amounts of energy are required to create surface in a bulk liquid and vapourise the dissolved gas. The mix head is the only place where sufficient energy is available for nucleation, so the action in the mix head directly affects the number of cells in the final foam. The manufacturer controls cell size by encouraging or inhibiting nucleation. These examples will describe how to change the manufacturing variables to produce a finer foam. It is possible to make a coarser foam by making the opposite change. The most reliable way to make a finer celled foam is to decrease the pressure in the mix head itself. Cells only nucleate in the mix head, and a low chamber pressure will make it easier to form gas bubbles from dissolved gas. Chamber pressure is normally controlled by the raw material pump settings and the diameter of the outlet pipe. Another way to make finer cells is to use raw materials that have a higher concentration of dissolved gas. These have more gas available to form nuclei, and will result in a finer foam. Surfactants also help create fine celled foam because the energy required to nucleate a bubble is directly proportional to the surface tension of the liquid [32]. Another way the manufacturer can nucleate more cells is to increase the energy input. This can be done by mixing at a higher speed [33] or by increasing the pressure of the line feeding raw materials to the mix head. Both of these changes will increase the pressure drop in the mix head, making it easier to cavitate cell nuclei from the available dissolved gas.

5.4.3 Growth Cell growth begins shortly after the liquid leaves the mix head as gas diffuses out of the liquid and begins to fill the bubble nuclei. The ambient external pressure is much lower than the mix head pressure so the bubbles can grow easily. In the early stages, bubbles are only a small part of the overall volume of the mixture (exception: liquid CO2 foams). They are far apart, and remain spherical. As they grow, the cells come in contact and must distort as they pack in three dimensions. Eventually gas will fill up to 99% of the total volume. Regions where two bubbles converge are called walls or membranes, while the intersections of three or more bubbles are called struts. Foam rises because the gases that are generated are trapped inside closed cells. The pressure inside the cells equals the external pressure plus the overpressure needed to maintain and grow the cells against the forces of gravity, friction, surface tension, viscosity 96

Flexible Polyurethane Foam and elasticity. The overall pressure in the cells drops significantly as the liquid leaves the pressurised mix head and will remain slightly above ambient during the free rise portion of the reaction. In a moulded foam, the pressure rises again as the mould is filled and the foam can no longer expand. In a free rise slabstock foam, the pressure in the cells remains slightly above atmospheric until the cell membranes rupture and gas vents to the atmosphere. If the stress of the expansion is too great, a large tear called a split may form inside the block. There are two potential sources for the blowing gas: chemically produced CO2 from the reaction of water and isocyanate, and volatile additives otherwise known as alternative blowing agents (ABA). Traditional ABA are low boiling compounds such as chlorofluorohydrocarbons (CFC), hydrofluorocarbons (HFC), methylene chloride, acetone [34] and hydrocarbons that evaporate at ambient pressure as the heat of exothermic isocyanate reactions causes the temperature to rise. More recently, machinery has been developed which allows the manufacturer to use liquefied CO2 as an ABA [35]. Of course, CO2 is a gas at ambient temperature and pressure, so it begins to vapourise as soon as the material leaves the mix head and external pressure drops to ambient. These foams form a froth that does not flow like a liquid. Therefore, they are laid on a slab conveyor as a ribbon that expands vertically with only slight growth in the horizontal direction. Bubbles in a liquid are thermodynamically unstable because they have a lot of surface area and therefore high surface energy. Further, the membranes are thinned by both cell growth and surface tension which pulls liquid from membranes into the struts. These factors destabilise the cell walls and make it more likely that they will rupture. It is important that cells do rupture (see Section 5.4.4), but they must remain closed through the growth phase because the pressure of the trapped gas supports the foam and makes it expand. This temporary stability comes from the surfactants and emulsifiers and is aided by the increase in viscosity as the polymer gels. Surfactants lower surface tension and reduce the surface energy needed to maintain the film. Emulsifiers prevent phase separation of dissimilar ingredients that could disrupt thinning membranes. Viscosity makes it more difficult for the liquid to flow, so the membrane is less likely to thin. When the destabilising factors finally overcome the stabilising influences the membranes rupture. Although the blow reaction will produce gas molecules for several minutes, the rise stops when the block vents to the atmosphere. Gas molecules produced after cell opening merely escape out of the foam.

5.4.4 Cell Opening In a flexible foam, cell opening is essential because closed cells lead to poor mechanical properties, low resilience and an undesirable pneumatic feel. In extreme cases, a closed cell flexible foam will shrink. At maximum rise, the cells are filled with hot gas, but as 97

Handbook of Polymer Foams the foam cools, the pressure inside drops. The membranes allow carbon dioxide to diffuse out faster than air diffuses in [36], so this further reduces pressure in cells that remain unopened after curing. The overall result is that a flexible foam with too many closed cells will shrink as it cools. To prevent shrinkage, some foams (notably moulded and high resilience slabstock types) are mechanically crushed to burst any closed cells. Rigid foams are strong enough to maintain a partial vacuum within each cell. These can have closed cells without shrinkage. Cell opening presents an interesting paradox. A microscope shows that cell membranes are often completely missing, indicating that the material had sufficient time and fluidity to flow completely into the strut. Yet at the time of cell opening, the polymer in the struts must be strong enough to maintain the cellular geometry and support the foam against the pull of gravity. Before cell opening, pressure in the cells supports the weight of the foam, but when the foam vents, the support must come from the struts. The foam will lose height (settle or sigh back) if the struts are not strong enough to support the weight above them. Over the years, several mechanisms of cell opening have been proposed, and it is likely that the exact cause of cell opening may be different in different types of foam. Probably the most comprehensive theory [37] begins with the precipitation of urea microdomains that signals the end of membrane stability. As this phase separation occurs, the polymer goes through a period where it exhibits extensional thinning behaviour [38]; that is, the viscosity drops dramatically as stress increases. If the polymer in the membrane is under higher stress, it can flow while the unstressed struts remain intact. There are two probable causes of this stress that will preferentially affect the membranes. One is driven by a pressure gradient known as the Laplace force that thins the membranes of all types of foam. The second is unique to polyurethane foams, where the precipitation of urea probably causes a sudden increase in density of the polymer. The polymer contracts, but the block of foam stays the same size. This gives a uniform force across the foam, but since stress is force per unit area, the membranes feel more stress because the crosssectional area is less.

5.4.5 Cure Once the cells open, the gas pressure is vented to the atmosphere. The foam is no longer supported by pneumatic means, yet gravity continues to pull the foam downward. At this point, the struts must have sufficient strength to support the weight of the foam or it will sag or settle under its own weight. As discussed in Section 5.4.4, it is important to balance the strength in the struts and instability in the membranes to control cell opening and ultimately determine the success of the foaming process.

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Flexible Polyurethane Foam As the polymer cures, the urea groups that form are attracted to each other because of their similar polarity and hydrogen bonding. Urea phase separation begins at cell opening and continues during the curing process. Urethane groups also phase separate as the polymer cures, so that the final polymer has distinct urea and urethane phases [39] dispersed in a ‘soft segment’ comprised mostly of less polar polyol chains. The urea and urethane phases contribute hardness and dimensional stability to the polymer because they are highly crystalline and remain intact well above room temperature. The continuous phase is the non-crystalline soft segment. When an FPF is compressed or elongated, the polyol chains in the soft segment can rearrange in response to the stress. Polyurethane elasticity is a result of the hard and soft segment morphology. It is important to recognise that although the foam achieves mechanical support after cell opening, it is far from having fully developed properties. The temperature continues to rise for several minutes beyond the cell opening, showing that isocyanate groups are still reacting. Both blow and gel reactions build molecular weight and add crosslinks to the polymer backbone. Since the cells have vented, gaseous products from the blow reaction simply escape to the atmosphere without contributing to any further foam rise. The mechanical properties of the foam improve as the curing reactions link together polymer chains and the temperature subsides. Large foam blocks are usually set aside for several hours before further processing, and final quality assurance testing is often delayed until the next day. Moulded foams can usually demould after a few minutes, but these also require several hours, often at elevated temperatures, to fully cure.

5.5 Manufacturing Equipment Over the years, FPF equipment and chemicals have evolved together. Current technology allows manufacturers to produce higher quality foams with less environmental impact and greater economy than ever before. New foam grades are now available that could not be made only a few years before, and that statement is likely to remain true far into the future. There are two main types of manufacturing equipment: slabstock machines that produce large, continuous blocks of foam (see Figure 5.4), and moulding machines that produce discrete parts which are cured in the shape and size of the mould. Both of these have three main systems. The first is the tanks, pumps, and pipes that store, meter and pump the raw materials, the second is the mix head, and the third takes the liquid pre-foam away from the mix head and provides the space for it to rise and cure.

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Figure 5.4 Typical block of slabstock FPF Source: Beamech

5.5.1 Storage and Delivery Moulded foam equipment is designed to accurately dispense relatively small amounts of liquid into each mould, so the feed tanks and delivery system are normally smaller and less complicated than those seen in a slabstock machine. A moulder may have dozens of machines, with each one running a few formulations. Additives are usually pre-blended and only 2-4 streams actually enter the mix head [40]. This is very different to slabstock machines which pour many different grades of foam. These can have twenty or more additive streams to accommodate the different formulas, each with its own storage, metering and delivery systems as detailed in Figure 5.5.

POLYOL

REQUIRED water catalyst surfactant

ISOCYANATE

OPTIONAL fillers flame retardants antioxidants colorants etc.

Figure 5.5 Schematic of slabstock mix head

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Flexible Polyurethane Foam

5.5.2 Mixing Years ago, slabstock and moulded foam machines both used a traditional mix head configuration. This is a cylindrical chamber where raw materials are introduced through ports along the sides and the liquid is mixed with a pin mixer on a rotating shaft. This design is ideally suited for slabstock foams because they operate continuously, but most moulded foams require a solvent flush after every shot. As environmental regulations have tightened, the impingement mix head was developed. This design forces together opposing jets of the raw materials and relies on turbulence to mix. Since there is no rotating shaft, the solvent flush is replaced by a plunger that purges the mixing chamber between shots [41].

5.5.3 Foam Rise and Cure The most obvious difference between moulded and slabstock machines is how they handle the liquid after it leaves the mix head. A moulded foam machine usually has many individual moulds that are attached to a carousel. Empty moulds are carried to the mix head, filled, closed and clamped. Most times, the mould is heated to accelerate the cure so that it can be opened sooner and readied for the next use. The foam parts need reasonable strength to demould, but they are often baked to complete the cure. In most slabstock machines, the liquid from the mix head is deposited on a paper covered conveyor with moving sides and an open top. Conventional foam machines (Figure 5.6) pour the liquid on the paper from above and allow it to spread across the conveyor

Figure 5.6 Conventional foam being poured Source: Beamech

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Handbook of Polymer Foams before it begins to froth. The conveyor is lowered through a series of fall plates that help to improve the foam profile. Foam from a conventional machine generally has a very uniform cell structure, but the blocks can have a crown in the middle because less liquid reaches the edges of the conveyor. Several innovations have been developed to eliminate the crown because rectangular blocks can be processed with much less cutting waste. Manufacturers can traverse the mix head to spread the liquid better. They can also use a device to lift the side paper while the foam is rising to raise the shoulders. With these improvements, good conventional foam is still limited to a size of approximately 2 metres wide and 1 metre high. Conventional equipment can also make round blocks of foam by using a conveyor with cylindrical side walls. A Maxfoam machine pumps the liquid into a trough that is almost as wide as the conveyor. As more liquid is pumped in, it spills out over the top so a uniform ribbon of froth is laid on the conveyor. In this case, the foam has a flat top because it expands in the vertical direction without spreading horizontally. As in conventional machines, the flattest blocks are made when fall plates lower the conveyor to nearly match the rise profile. The Maxfoam system can produce large blocks with a good rectangular shape, but the turbulence in the trough adversely affects cell structure. Recently, machines have been introduced that can quickly switch between conventional and Maxfoam configurations to improve operational flexibility [42] (see Figure 5.7).

Figure 5.7 Schematic showing conventional and Maxfoam capabilities Source: Beamech

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5.5.4 Innovations Equipment for large-scale polyurethane foam manufacturing has become much more automated and sophisticated over the years, but in most cases, the difference between machines from the 1960s and today relate to computerisation rather than the engineering principle. All parts of the system are now more precisely controlled by a centralised computer that can store hundreds of different formulations and allows the manufacturer to change between foam grades with a single command [43]. The most notable equipment inventions of the past decade are VPF, CO2 as a blowing agent and ground foam recycling. VPF and CO2 are both aimed at production of lower density slabstock foams without the use of regulated blowing agents. For many years, soft, safe low density foams were made by adding CFC or methylene chloride to the formulation, but environmental regulations severely restricted these additives. Chemical companies developed less harmful blowing agents, but most are flammable or expensive and can still have environmental concerns. Low density, all-water blown foams are not as soft and may be dangerous to produce because the exotherm temperature can exceed the fire point. Rapid cooling strategies were adopted [44, 45] to reduce the fire danger, and more recently, the equipment industry developed two elegant solutions: VPF and CO2. The entire foam conveyor of a VPF machine is enclosed in a large vacuum chamber [46]. Foams made at reduced pressure have a lower density because the same amount of blowing gas will fill a larger volume. Therefore, VPF machines can produce soft, low density foams with a moderate exotherm and without blowing agents [47]. Another advantage is that they collect and treat the toxic gases before releasing them to the atmosphere. Some VPF machines may be operated above ambient pressure to produce unique foam grades. Carbon dioxide blown foam technology was developed at around the same time as VPF, and has been used extensively to make both slabstock and moulded foams. Of course, carbon dioxide is a gas at ambient conditions, and low temperature and high pressure are used so that it can be introduced into the mix head as a liquid [48]. CO2 remains a liquid in the pressurised mix head, but it will vapourise as soon as the mixture exits [49]. The successful implementation of this technology required significant effort to develop hardware that would smoothly transition the pressure to ambient without stressing the liquid [50]. The froth leaves the mix head through a precisely engineered, narrow slot which is almost as long as the conveyor width. The froth flows poorly, so the most of the foam expansion should be in the vertical direction as in a Maxfoam machine. Another recent innovation allows the manufacturer to non-cryogenically grind foam scrap from the manufacturing process. The ultrafine powder is then used to displace more than 20% of the virgin chemicals in the manufacture of new foam. With minor

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Handbook of Polymer Foams formulation adjustment, the resulting foam has properties equal to the original foam, so the economics are driven by the difference between the value of scrap and the price of chemical raw materials. The declining use of scrap foam in North American carpet cushion has improved the economic advantage and led to its rapid adoption. As this technology becomes more widespread, it will also allow the recycling of significant amounts of postconsumer foams that currently end up in landfills [51].

5.6 Foam Characterisation There are many tests used to measure the properties of FPF. The most significant methods are formalised under ASTM D3574 [52] and D3453 [53] and BS EN ISO 1798 [54]. In 1994, the Polyurethane Foam Association (USA) published the Joint Industry Foam Standards and Guidelines [55] which relates the test data to foam performance and value, particularly in the furniture industry. Of course, there are many tests that are specific to a particular customer, manufacturer or application. Some of the more important tests are summarised in the next section.

5.6.1 Density Density and hardness are sometimes thought to be similar, but these are completely different properties, and surprisingly, there is only a weak relationship between them [56]. Adding water to reduce density also increases the amount of urea in the polymer which makes it harder. Many flame retardants increase density while softening the foam, and copolymer polyols will stiffen the foam without affecting density. Density is important to the performance and economics of a foam because it measures how much of a foam is air and how much is polymer. The density is simply the mass divided by the volume and is commonly measured in kilograms per cubic meter (kg/m3) [57]. Most conventional grades of slabstock foams range from about 12 to 40 kg/m3. Foams with fillers, flame retardants and copolymer or polyester polyols usually have a higher density and range from 25 to 100 kg/m3. Flexible moulded foams can be poured in much higher densities, but they can also go down to about 25 kg/m3 [58].

5.6.2 Hardness Hardness is very important because most foams are used in applications where they provide at least some type of cushioning. Therefore it is important to know how much force is required to give a particular deflection or how much weight it can support.

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Flexible Polyurethane Foam Harder foams are produced by increasing the isocyanate index, using copolymer polyols or adding fillers [59]. High density moulded foams can be measured with a hand held durometer which has a small indenter foot attached to a deflection spring. It measures the force required to push the foot into the foam a known depth. The base of the durometer is only a few centimetres across, and the deflection is just a few millimetres so it is useful for small samples but only marginally accurate on slabstock foams. Larger foam samples are usually measured by either the indentation force method (IFD) [60] or the compression force deflection (CFD) [61] methods. Both tests use a large foot (normally 325 cm2). A CFD test uses a foam block smaller than the foot. This eliminates friction effects and allows the foam to flatten horizontally. IFD uses a large 10 cm thick block of foam so that the circular foot is smaller than the sample. In both tests, the force is measured at various deflections. There are many variants of this test depending on the application. For the furniture industry, the most commonly reported values are the 25% IFD and 65% IFD (IFD measured at 25% or 65% compression), and furniture foam is normally specified by density and IFD. There are also other values derived from IFD. For example the guide factor is IFD divided by density. Compression modulus is the ratio of 65% IFD to 25% IFD. In seating applications compression modulus is called support factor because higher values indicate that the foam feels soft yet can support more weight without bottoming out. A hysteresis value is calculated after running 25% IFD, 65% IFD and then a second 25% IFD on the same piece of foam. The loss of 25% IFD after the 65% compression is the hysteresis.

5.6.3 Resilience Resilience is measured by dropping a steel ball on a foam sample and measuring the height of the rebound [62]. The ball rebound test is different from the hardness tests because it indicates the instantaneous feel of the foam. The FPF industry quickly recognised that resilience was important for many applications, and high resilience (HR) foams were defined under ASTM D3770 [63]. Special copolymer polyols for HR foams were introduced in the 1960s [64], and these now constitute a significant part of the overall FPF industry. EO capped polyether polyols with modified polyisocyanates are also used [65, 66]. More recently, low resilience foams have also gained in importance [67, 68]. These are known as viscoelastic, slow recovery or energy absorbing foams and will give a characteristically low value on a ball rebound test. There are many ways to formulate viscoelastic foams, although most are made with MDI. The key is to reduce polymer elasticity around room temperature. Some techniques known to produce viscoelastic

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Handbook of Polymer Foams foams include the use of low molecular weight crosslinkers, blends of incompatible polyols, alkoxylated alcohols, foreign polymers, plasticisers, and variations of isocyanate index [9]. In any of these tests, one must realise that foam will soften as temperature and humidity increase [70]. In slabstock foams, hardness also varies across the height and width of the block, and is even affected by whether the sample was cut in the horizontal or vertical direction relative to the rise.

5.6.4 Porosity Filtering, acoustic and gasketing applications usually require that the foam either permits or blocks the passage of air. End users of other types of foam are not usually concerned about porosity per se, but foam manufacturers have long known that air flow is by far the easiest way to approximate the amount of intact cell windows in the foam, and this affects many other important properties. Increasing porosity normally leads to better resiliency and mechanical properties, but it is more difficult to produce high porosity, low density foam because cell opening occurs earlier in more porous foams, so more of the blowing gas is lost to the atmosphere. The surest way to produce foams with very high air flow is by chemically or physically destroying all residual membranes after the foam is cured. These reticulated foams are excellent for applications such as filtration, or liquid delivery where membranes will interfere with the flow of air or liquid through the foam. The traditional way to determine porosity is to measure the air flow in m3/second needed to maintain a pressure differential of 125 Pa on a standard sized 50 mm x 50 mm x 25 mm [71] piece of foam. It is also possible to measure the pressure drop that occurs when pulling a known volume of air through a cross sectional area of the foam. Open celled foams give high numbers in the first method and low numbers in the second. Like hardness, porosity can be significantly different in the horizontal and vertical directions.

5.6.5 Strength Properties Hardness indicates the force needed to compress a foam. Tensile and tear strength measure the force required to stretch and tear a foam respectively. Therefore, hardness is important in cushioning, and tensile and tear strength are important when the foam is stretched in handling or use. Tensile, tear and elongation are usually mentioned together because they are all run on an extensometer, and differ only in the sample preparation. This device has two jaws which hold the specimen and measure the force while slowly pulling it apart. In principle, these measurements are the same for foams as for any other material. The difference is that foams are not regular on a small scale, so much larger specimens

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Flexible Polyurethane Foam must be used to compensate for the irregularity. The tensile experiment uses a classic ‘dumbbell’ or ‘dog bone’ shaped sample and measures the force per unit area (at the narrow part of the specimen) required to break the sample. The increase in length at this point is the elongation and is reported as a percentage of initial length [72]. Sometimes, the force at 100% elongation is also recorded as the 100% modulus. In the foam industry, tear strength is normally measured on a ‘split tear’ specimen. This requires a rectangular sample with a cut down the centre. The foam is torn apart by pulling opposite sides of the cut apart. Tear strength is the force required to continue tearing the foam. It is measured as force per linear centimetre of the cut [73].

5.6.6 Cell Structure Technical applications often require foams with a particular cell size or structure. It is easy to recognise the difference between large and small cells, but it is more difficult to agree on an exact measurement because a close look reveals the difficulty in measuring a three dimensional cell with a ruler. Further, most cells have a slightly elongated shape. Today, the cell size of most foams is measured by eye using a linear cell count method. Methods that compare images of the foam to circular standards are more accurate and less dependent on the individual running the test, but require more sophisticated equipment [74, 75]. Cell uniformity can be even more subjective than cell size. Customers normally expect the cells in a piece of foam to all be about the same size. Contaminants or air holes can cause obvious non-uniformity, and can immediately turn the block to scrap. Some applications demand a very consistent structure, but if the foam is hidden, there is considerably more leeway. Some types of foams are intentionally contaminated to give a consistent non-regularity to imitate the appearance of natural sea sponge. As with other appearance issues, the manufacturer and customer usually develop an informal understanding about what good foam looks like.

5.6.7 Environmental Stability Stability and resistance tests are designed to determine if the foam will continue to deliver expected performance throughout its working life. Many foams are used in environments that can degrade foam quality. Some examples would be exposure to water [76], microorganisms, oil, solvents, high temperatures [77], sunlight and so on. There are many different stability tests depending on the type of foam and its intended use. In general they involve measuring the properties of interest, (e.g., hardness, tear strength, colour, size) on a foam sample before and after controlled exposure to the degradative element.

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Handbook of Polymer Foams By increasing temperature or severity, it is often possible to estimate the effect of years of ageing in a few weeks [78].

5.6.8 Fatigue Many types of foam, such as those used in carpet cushion and seating applications are expected to provide excellent cushioning properties for years of continuous use. Fatigue resistance is clearly important in carpet padding, upholstered furniture and automotive seating, but the foam thickness, compressive force, and sliding motion in each application is quite different. Literally dozens of fatigue methods have been developed over the years that attempt to mimic a particular end use. All dynamic fatigue tests put a foam sample through thousands of compression cycles and measure softening and thickness loss. Some also add a sliding or rolling element to simulate the other forces that a cushion will see in normal use. ASTM D3574 [52] lists three fatigue methods [79]. One is a static test that measures the decrease in force needed to maintain a constant deflection over time. The other two are dynamic tests which either use a constant force pounding or a constant force compression with a rolling component [80]. Generally, higher density foams perform better in dynamic fatigue tests [81].

5.6.9 Compression Set Compression set tests are similar to static fatigue methods except that they normally run at much higher temperatures and can also include humidity, either as a preconditioning step or during the test [82]. Foams can be permanently compressed to a fraction of their original height if the temperature is high enough. These ‘felted’ foams are useful in certain filtration or liquid delivery applications.

5.6.10 Flammability Numerous disclaimers should precede this discussion of FPF flammability. As a general summary, it is meant to offer an insight into the topic. The information presented herein is believed to be factual, but the reader is warned that regulations and methods change regularly and may not apply in a particular marketplace or geographical region. It is presented without warranty and should only serve to direct interested readers to more definitive sources of information. Flammability testing regulations are exceedingly complex, with numerous governmental and private agencies imposing standards for foams which fall under their auspices.

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Flexible Polyurethane Foam Polyurethane foam flammability has been studied in great detail [83, 84]. While much has been learned since the early days of the industry, fire is almost always accidental, so it is impossible to predict how it will start or how it will spread. The best we can do is come up with tests that are expected to model most likely scenarios. These include different ignition sources, foam sizes and orientations, and may or may not include other materials such as fabric in composite structures [25, 85]. As the industry becomes more global, a few tests have emerged that have broad acceptance. Automotive foams are almost always certified to MVSS 302 [86] or its near equivalent DIN or JIS standards. Furniture foams are usually tested by California TB-117 (residential, component testing) [87] and Cal TB-133 (public occupancy, composite testing) [21] in North America or BS 5852 (furniture) [23] and BS 7177 (mattresses) [88] in Europe [89]. It is likely that Cal TB-117 will move toward composite testing in the near future [87] to harmonise it with the British Standard test. Other regional specifications also exist [90] including the Boston Chair, New York Subway, and Italian Railway tests. Aircraft and other military foams sometimes require a Military Specification (Mil Spec) test, and packaging foam normally falls under UL94HF1 [91, 92]. As a last word, the reader is reminded that no test is completely reliable at predicting fire performance under a particular set of conditions.

5.7 FPF Markets The global market for FPF is estimated at over 3 million tonnes, roughly divided between the Americas, Europe-Africa and Asia-Pacific. Of these, Asia-Pacific has shown the highest growth rate [93]. Table 5.2 breaks down production by foam type and geography. There are thousands of uses for FPF ranging from commodity cushioning products to highly specialised technical foams. The transportation and furniture industries are the two largest

Table 5.2 Estimated foam production in 2001 Tonnes foam

Asia-Pacific

Europe-Africa

Americas

Global

Polyether

530,000

620,000

880,000

2,030,000

HR

90,000

180,000

140,000

410,000

Polyester

60,000

120,000

60,000

240,000

Total Slab

680,000

920,000

1,080,000

2,680,000

Moulded

270,000

380,000

330,000

980,000

Total FPF

950,000

1,300,000

1,410,000

3,660,000

Source: IAL Consultants

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Handbook of Polymer Foams consumers for FPF, and carpet cushion and packaging are also major markets [94]. While all other foam applications only comprise approximately 10% of the foam produced, these cover a broad range of specialty products that tend to have more stringent requirements, and come with concomitantly higher profitability.

5.7.1 Transportation Automotive and other transportation applications are clearly the largest markets for moulded foam, and also use considerable amounts of slabstock foam. Automotive foams use a higher percentage of MDI than the other markets. Within this segment, FPF is used for seating, components (such as head and arm rests), textile lamination, gasketing, filtration, sound absorption, and energy management. As a group, automotive foams tend to require durability, high and low temperature resistance and hydrolytic stability. Volatile compounds such as the antioxidant butylated hydroxy toluene (BHT) must be eliminated from automotive foams because they can condense on the glass and cause a hard-to-clean fog on windows [95]. These foams are often required to meet the fire resistance of MVSS-302 [85] or other similar worldwide standards.

5.7.2 Comfort The combined furniture and bedding industries are the largest user of slabstock foams and also consume considerable amounts of HR foam. These industries are highly dependent on the economy and its effect on disposable income [96]. The foams tend be the lowest density products that give adequate support and fatigue resistance. Polymer polyols are important here as they increase hardness and resilience without changing density [97]. Depending on the location of the cushion, different factors contribute to the overall perception of comfort. For example thick seat cushions and back cushions tend to be softer, while thin seat cushions and bedding foams are usually harder. The bedding industry is now becoming a major user of viscoelastic foams that conform to the weight of the body and offer more uniform support [98]. Flammability is also a major issue in furniture and bedding foams, and a number of appropriate standards may apply.

5.7.3 Carpet Cushion Carpet cushioning foams are a North American phenomenon, as this application is almost non-existent in the rest of the world. These can be high density prime or rebond foam. In North America, most manufacturing remnants are recycled into carpet cushion. This

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Flexible Polyurethane Foam process entails shredding the foam and bonding the bits together with an isocyanate binder. This high density composite gives excellent durability, improves comfort and reduces noise and carpet wear [99].

5.7.4 Packaging In an industry dominated by paper products, cloth, natural materials and other foamed polymers, FPF maintains an important position in the packaging industry. Foam is often considered a high-end choice because it can be shaped to the contours of delicate parts and gives good aesthetics, excellent protection and light weight. Foam hardness, resilience, air flow [100] and sample geometry [101] all affect the cushioning properties of FPF. A packaging engineer will choose an appropriate foam by considering the fragility of the object, anticipated loads, weight and space requirements [102].

5.7.5 Specialty Applications There are thousands of niche FPF products with higher technical requirements and lower production volumes that are grouped together as the technical foams. These often require very specific cell size or cell structure, porosity, hardness, solvent or water resistance, diffusion properties, elongation, strength or compatibility with specific chemicals. Technical foams are more likely to use polyester polyols because they give a uniform cell structure and the cell size is easier to control. They are also stronger and give better solvent resistance. They often go through one or more post processing steps to enhance one or more of these properties. Reticulation refers to the chemical or thermal opening of cell membranes to leave a network of polymer which will pass air with very little resistance. Reticulated foams are commonly used in filtration. Felting is a process which permanently compresses the foam with heat and pressure to give a densified foam that is particularly good at wicking and transporting liquids.

5.8 Environmental Issues In today’s world, most industries have had to answer questions about the environmental impact of their products. The FPF industry is no exception, and despite a long history of significant gains, there is still room for improvement. In fact, more than half of the papers presented at the Polyurethane Foam Association (PFA) meetings since 2000 have dealt with safety or environmental issues [103]. Many fair concerns have been raised, while other claims are based on perception rather than science and the critics aim to try

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Handbook of Polymer Foams the industry in the court of public opinion. Often, spurious claims do more harm than good because they distract the industry and the public from meaningful issues that could be improved. In all, the environmental stakeholders can be divided into four groups: plant workers, neighbours, consumers and the general public. Today, many companies in the FPF industry adhere to Responsible Care® (registered trademark of the American Chemistry Council) guidelines that make safety and environmental considerations an integral part of the decision making process [104]. Plant workers are mainly concerned about the dangers they face during their working lives. This includes acute and chronic effects of the chemicals that are used in the manufacturing process as well as potential hazards from physical dangers such as falling objects, cutting saws, falls, fires and other aspects of the manufacturing environment. Workplace safety is primarily the responsibility of owners, management, and the workers themselves. Organisations such as the Occupational Health and Safety Association, (OSHA) in the USA, establish national safety standards for the workplace. These tend to be stricter in developed nations. Any manufacturing site has unanticipated dangers, but as the industry matures, the hazards become clearer and safer procedures and equipment protect workers better. None of this is unique to the FPF industry. The main specific hazard to FPF workers and people living near factories comes from the vapours of isocyanates and other chemicals used in the process. In the USA, emission standards are established by the Environmental Protection Agency (EPA) [105]. Toxicological information on any chemical should be obtained from a Materials Safety Data Sheet (MSDS), but the industry has generally been most concerned with TDI , and continues to study its properties [106]. A recent study in the USA showed that TDI vapours close to the rising and curing foam occasionally exceed American Conference of Governmental Industrial Hygienists (ACGIH)/OSHA limits, but respiratory protection makes actual worker exposure rare [107]. New technologies more efficiently collect and treat process gases [108-110], and a number of non-fugitive additives have been developed [111-113]. Despite the continuing improvement in air quality both inside manufacturing plants and in nearby areas, neighbourhood complaints have arisen. In 1997, these led to the closure of the Trinity American Corporation’s facility in North Carolina, USA. Later, the diisocyanate panel of the American Chemistry Council reviewed the data and concluded that there was no scientific or legal basis for closing the plant [114]. Consumers expect products to be safe. FPF is lightweight and soft so it does not present any physical hazards. Flammability is certainly a legitimate issue, and was discussed earlier in Sections 5.3.9 and 5.6.10. The industry has extensively studied the potential for toxic chemical exposure through contact with FPF. TDI has not been found in the product, and none of the other emissions occur at concentrations that pose significant health risks to humans under normal use conditions [115]. There is no positive evidence

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Flexible Polyurethane Foam that chemicals emanating from FPF harm consumers, yet advocacy groups occasionally raise concerns. Over the past decade, use of BHT, butyl tin catalysts, volatile amines, nonylphenol ethoxylates and various flame retardant chemicals have all been questioned, and in all cases, the industry has found alternatives. A widely publicised report that the suspected carcinogen toluene diamine is found in aged foam samples [116, 117] has been shown to be the result of an analytical error [118, 119]. The FPF community has continued to develop technologies that reduce the impact of manufacturing on the global environment. In 1987, the Montreal Protocol called for CFC elimination by the year 2000, and this work was completed well ahead of schedule. Other harmful ABA have also been reduced by chemical and mechanical innovations [120]. Nearly all manufacturing trimmings are recycled into rebonded carpet cushion foams [121]. The vast majority of foams that end up in the environment come from consumers. There are many possible fates including litter, landfill, incineration, or recycling. Alliance for the Polyurethane Industry (API) has shown that foams are safe in landfills. Degradation is minimal, and they do not contaminate groundwater [122]. A study by Polyurethane Recycle and Recovery Council (PURRC) demonstrated that municipal incineration is also a safe and viable option for energy recovery [123]. Incineration is also recommended by the European Isocyanate Producers Association (ISOPA) [124]. Recycling is the best option as it uses foam wastes to make new products. There is already a large market for scrap foam as a raw material for rebonded products in North America. European legislation is expected that will preclude disposal of FPF in landfills and mandate recycling, particularly in automotive applications. If enacted, the amount of scrap should significantly outpace demand for rebond. One possibility is to recycle scrap foam by glycolysis which chemically reconstitutes it into new raw materials [125]. Another method grinds the scrap into a fine powder that can be reintroduced into foam production, reducing the need for virgin raw materials. This technology is already used to recycle manufacturing trimmings, and it is likely to be applied to post consumer scraps as the equipment becomes more widespread [53].

5.9 Organisations Four industry trade organisations are specifically dedicated to FPF. The PFA (www.pfa.org) and the Alliance for Flexible Polyurethane Foams (AFPF), (www.afpf.com) are based in North America. Many European countries have national FPF organisations, and the national groups together make up Europur (www.europur.com). The fourth FPF organisation is the Japan Urethane Foam Association (JUFA). Other trade associations

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Handbook of Polymer Foams are involved in the FPF community as part of their broader scope, including ISOPA, API, PURRC and International Isocyanate Institute (III).

References 1.

O. Bayer, Angewandte Chemie, 1947, 59, 257.

2.

Personal discussion with Angela Austin of IAL Consultants, 2003.

3.

E. Grigat and D. Dieterich in Polyurethane Handbook, 2nd Edition, Ed., G. Oertel, Hanser Publishers, New York, NY, USA, 1993, p.12.

4.

J.M. Hugo, M.W. Spence and T.D. Lickly, Proceedings of the Polyurethane Foam Association Technical Program, Williamsburg, Virginia, USA, October 1997, Paper No.10.

5.

R.E. Stevens, G.P. Dado, M.J. Kimock and M.L. Listemann, Proceedings of the SPI Polyurethenes World Congress, Amsterdam, The Netherlands, 1997, p.118.

6.

M.L. Listemann, A.C. Savoca and A.L. Wressell, Proceedings of the SPI Polyurethanes World Congress, Nice, France, 1991, p.524.

7.

L.F. Lawler and R. Schiffauer, Proceedings of the SPI Polyurethanes World Congress, Vancouver, BC, Canada, 1993, p.288.

8.

E. Cassidy, P. Chaffanjon and R. Lockwood, Proceedings of the SPI Polyurethanes World Congress, Amsterdam, The Netherlands, 1997, p.55.

9.

A. Parfondry in The Polyurethanes Book, Ed. D. Randall and S. Lee, John Wiley & Sons, New York, NY, USA, 2002, Chapter 14, p.221.

10. W. Hahn in Polyurethane Handbook, 2nd Edition, Ed., G. Oertel, Hanser Publishers, New York, NY, USA, 1993, p.23. 11. Joint Industry Foam Standards and Guidelines, Section 15, Glossary of Flexible Polyurethane Technology, Polyurethane Foam Association, Knoxville, TN, USA, 1994. 12. J.M. Monso, J. Soler, P. Escobar and C. Fernandez-Llamazares, Proceedings of UTECH 94 Conference, The Hague, The Netherlands, 1994, Paper No.47. 13. B. Kanner and T. Decker, Journal of Cellular Plastics, 1969, 5, 1, 32.

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Flexible Polyurethane Foam 14. K. Diblitz and C. Diblitz, Proceedings of the SPI Polyurethanes World Congress, Vancouver, BC, Canada, 1993, p.619. 15. M.L. Listemann, A.L. Wressell, K.R. Lassila, H.C. Klotz, G.L. Johnson and A.C. Savoca, Proceedings of the SPI Polyurethanes World Congress, Vancouver, BC, Canada, 1993, p.595. 16. M. Clauss, S.M. Andrews, J.H. Botkin and L. Macena, Proceedings of the SPI Polyurethanes Expo, Las Vegas, NV, USA, 1996, p.156. 17. J. Sturgeon, Proceedings of the Polyurethane Foam Association Technical Program, Salt Lake City, UT, USA, October 2002, Paper No.16. 18. Personal discussion with Richard Rose of Great Lakes Chemical, 2003. 19. H. Creyf, Proceedings of the Polyurethane Foam Association Technical Program, Arlington, VA, USA, May 2002. 20. B.L. Carson, Toxicological Summary for Selected Polybrominated Diphenyl Ethers, National Institute of Health, Bethesda, MD, USA, 2001. 21. T. Geran, Proceedings of the Polyurethane Foam Association Technical Program, Salt Lake City, UT, USA, October 2002, Paper No.13. 22. Technical Bulletin No.133, Flammability Test Procedure for Seating Furniture for Use in Public Occupations, California Bureau of Home Furnishings and Thermal Insulation, 1991. 23. BS 5852, Methods of Test for Assessment of the Ignitability of Upholstered Seating by Smouldering and Flaming Ignition Sources, 1990. 24. M. Barker, M.P. Hannaby and F.J. Lockwood, Proceedings of the SPI Polyurethanes World Congress, Nice, France, 1991, p.628. 25. Personal discussions with Dave Kelly of William T. Burnett and Dimitri Dounis of Hickory Springs, 2003. 26. H. Stone, Overview of the Combustibility and Testing of Filling Materials and Fabrics for Upholstered Furniture, 1998, PFA, Wayne, NJ, USA. 27. M. Kageoka, Y. Tairaka and K. Kodama, Proceedings of the SPI Polyurethanes World Congress, Chicago, IL, USA, 1995, p.62.

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Handbook of Polymer Foams 28. G. Howard, Proceedings of the Polyurethane Foam Association Technical Program, Scottsdale, AZ, USA, October 1996, Paper No.1. 29. A.B. Lehnert, Proceedings of the SPI Polyurethanes World Congress, Las Vegas, NV, USA, 1996, p.98. 30. L. Jung, Proceedings of the SPI Polyurethanes World Congress, Nice, France, 1991, p.169. 31. Personal discussion with Rob Borgogelli of Goldschmidt, 1999. 32. T. Housel, Proceedings of the Polyurethane Foam Association Technical Program, San Diego, CA, USA, October 1999, Paper No.4. 33. R. Baumhäkel, Journal of Cellular Plastics, 1972, 8, 6, 304. 34. Hickory Springs Manufacturing Company, Proceedings of the SPI Polyurethanes World Congress, Amsterdam, The Netherlands, 1997, p.740. 35. C. Fiorentini, M. Taverna, B. Collins, C. Greaves and T. Griffiths, Proceedings of the Polyurethane Foam Association Technical Program, Newport, RI, USA, October 1994, Paper No.10. 36. M. Olsson, Long-term Thermal Performance of Polyurethane Insulated District Heating Pipes, Chalmers University of Technology, Gothenburg, Sweden, 2001, p.33. [PhD Thesis] 37. T. Housel, Urethanes Technology, 2001, 18, 5, 40. 38. X.D. Zhang, H.T. Davis and C.W. Macosko, Journal of Cellular Plastics, 1999, 35, 5, 458. 39. J. Mertes, H. Stutz, W. Schrepp and M. Kreyenschmidt, Proceedings of the SPI Polyurethanes World Congress, Amsterdam, The Netherlands, 1997, p.46. 40. Mixing Heads, Linden-EMB Technical sales literature, Linden Industries, Inc./ EMB, Cuyahoga Falls, OH, USA, 2002. 41. Introduction to Polyurethane Equipment, Cannon seminar, Mars, PA, USA, 1993. 42. Ultima Felxible Slabstock Foam Equipment, Beamech Ultima literature, Beamech, Manchester, UK, 2000.

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Flexible Polyurethane Foam 43. J. Rayner, Proceedings of UTECH Asia, Suntec City, Singapore, 1999, Paper No.2. 44. M.A. Ricciardi and D.G. Dai, Proceedings of the Polyurethane Foam Association Technical Program, Point Clear, AL, USA, 1992, Paper No.6. 45. H. Stone, E. Reinink, S. Lichvar, G. Rusenko, W. Carlson, and C. Sikorski, Proceedings of the Polyurethane Foam Association Technical Program, Point Clear, AL, USA, 1992, Paper No.8. 46. R. Triolo, Proceedings of the Polyurethane Foam Association Technical Program, Quebec City, Quebec, Canada, 1993, Paper No.10. 47. D. Ramazzotti and S. Carson, Proceedings of the SPI Polyurethanes Conference, Boston, MA, USA, 1994, p.8. 48. M. Taverna, Proceedings of the SPI Polyurethane Expo, Las Vegas, NV, USA, 1996, p.370. 49. B. Blackwell, G. Buckley and W. Blackwell, Proceedings of UTECH Asia, Suntec City, Singapore, 1997, Paper No.48. 50. T. Griffiths, Proceedings of the Polyurethane Foam Association Technical Program, Salt Lake City, UT, USA, 2002, Paper No.3. 51. Personal communication with Martin Dawson of Mobius Technologies, 2003. 52. ASTM D3574, Test Methods for Flexible Cellular Materials – Slab, Bonded and Molded Urethane Foams, 2001. 53. ASTM D3453, Standard Specification for Flexible Cellular Materials – Urethane for Furniture and Automotive Cushioning, Bedding and Similar Applications, 2001. 54. BS EN ISO 1798, Flexible Cellular Polymeric Materials – Determination of Tensile Strength and Elongation at Break, 2000. 55. Joint Industry Foam Standards and Guidelines, PFA, Knoxville, TN, USA, 1994. 56. Joint Industry Foam Standards and Guidelines, Section 1.0, Density Standards and Guidelines, Polyurethane Foam Association, Knoxville, TN, 1994. 57. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test A: Density Test, 2001. 117

Handbook of Polymer Foams 58. K. Usaka, M. Isobe, H. Utsumi and K. Ohkubo, Proceedings of the API Polyurethanes World Congress, Salt Lake City, UT, 2002, p.75. 59. D.R. Gier, R.E. O’Neill, M.R. Adams, R.D. Priester, W.A. Lidy, C.G. Barnes, E.G. Rightor and B.L. Davis, Proceedings of the SPI Polyurethanes World Congress, Dallas, TX, 1998, p.227. 60. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test B1:Indentation Force Deflection Test – Specified Deflection, and Test B2: Indentation residual Gage Load Test – Specified Force, 2001. 61. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test C: Compression Force Deflection Test, 2001. 62. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test H: Resilience (Ball Rebound) Test, 2001. 63. The Furniture Industry’s Guide to Today’s Flexible Polyurethane Foam, AFPF, USA, 1996, p.13. 64. W.C. Kuryla, F.E. Critchfield, L.W. Platt and P. Stamberger, Journal of Cellular Plastics, 1966, 2, 2, 84. 65. D. Hicks, G. Davies, S. Spertini and P. Chaffanjon, Proceedings of UTECH 2000, The Hague, The Netherlands, 2000, Innovations: Flexible Foam Development Session, Paper No.3. 66. S. Murakami, K. Saiki, M. Hayashi, T. Satou and T. Fukami, Proceedings of the API Polyurethanes Conference, Boston, MA, USA, 2000, p.281. 67. S. Narayan and A. Berube, Proceedings of the API Polyurethanes Expo, Columbus, OH, USA, 2001, p.201. 68. P. Farkas, R. Stanciu, and L. Mendoza, Proceedings of the API Polyurethanes Expo, Columbus, OH, USA, 2001, p.143. 69. A. Parfondry in The Polyurethanes Book, Ed. D. Randall and S. Lee, John Wiley & Sons, New York, NY, USA, 2002, Chapter 14, p.220. 70. Joint Industry Foam Standards and Guidelines, Appendix A3.0, Temperature and Humidity Effects on IFD, Polyurethane Foam Association, Knoxville, TN, 1994, Section 3.1.

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Flexible Polyurethane Foam 71. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test G: Air Flow Test, 2001. 72. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test E: Tensile Test, 2001. 73. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test F: Tear Resistance Test, 2001. 74. Visiocell – A New Method to Measure the Cell Diameter of Polyuretahne Foam, Recticel Visiocell Technical literature, Recticel, Wetteren, Belgium, 1999. 75. K.M. Lewis, I. Kijak, K.B. Reuter and J.B. Szabat, Proceedings of the SPI Polyurethanes World Congress, Vancouver, BC, Canada, 1993, p.517. 76. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test L: Wet Heat Aging, 2001. 77. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test K: Dry Heat Aging, 2001. 78. J.T. McEvoy and R. Yamasaki, Proceedings of the API Polyurethanes Expo, Columbus, OH, USA, 2001, p.281. 79. ASTM D3574, Standard Test Methods for Flexible Cellular Materials – Slab, Bonded and Molded Urethane Foams, 2001. 80. Joint Industry Foam Standards and Guidelines, Section 9.0, Standards and Guidelines for Dimensional Tolerances of Polyurethane Foam, Polyurethane Foam Association, Knoxville, TN, 1994. 81. J.E. Knight, Proceedings of the SPI 30th Annual Technical/Marketing Conference, Toronto, Canada, 1986, p.48 82. D3574-01, Standard Test Methods for Flexible Cellular Materials—Slab, Bonded, and Molded Urethane Foams, Test D: Constant Deflection Compression Set Test, 2001. 83. E. Bleuel, P. Boehme, U. Rotermund, M. Reichelt and C. Seitz, Proceedings of the API Polyurethane Conference, Salt Lake City, UT, USA, 2002, p.234. 84. B. Bastin, R. Paleja and J. Lefebvre, Proceedings of the Polyurethane Foam Association Technical Program, Salt Lake City, UT, USA, October 2002, Paper No.15.

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Handbook of Polymer Foams 85. J. David, Assessing the Need for a Federal Small Open Flame/Cigarette Ignition Upholstered Furniture Flammability Standard, National Economic Research Associates, San Francisco, CA, USA, 2001. 86. MVSS 302, Flammability of Interior Material – Passenger Cars, Multipurpose Passenger Vehicles, Trucks and Buses, 1972. 87. Technical Bulletin No. 117, Requirements, Test Procedure and Apparatus for Testing the Flame Retardance of Resilient Filling Materials Used in Upholstered Furniture, California Bureau of Home Furnishings and Thermal Insulation, North Highlands, CA, USA, 2000. 88. BS 7177, Specification for Resistance to Ignition of Mattresses, Divans and Bed Bases, 1996. 89. InTouch, 1999, 7, 1, 4. 90. International Association of Fire Fighters & The National Association of State Fire Marshals, Safety Alert Bulletin, 1999, 1, 1, 1. 91. UL 94HFI, Standard for Tests for Flammability of Plastic Materials for Parts in Devices and Appliances, 1996. 92. Personal discussion with Richard Rose of Great Lakes Chemical, 2003. 93. Data provided by IAL Consultants, London, 2002. 94. End-Use Market Survey on the Polyurethane Industry in the USA, Canada and Mexico in 2000, API, Arlington, VA, USA, 2001. 95. D.J. Grillo, T.L. Housel and F.A. Landis, Proceedings of the Polyurethane Foam Association Technical Program, Newport, RI, October 1994, Paper No.1. 96. B. Poole, Proceedings of UTECH, 2000, The Hague, The Netherlands, Furnishings Session, Paper No.1. 97. InTouch, 1995, 5, 1, 3. 98. L. White, Urethanes Technology, 2001, 18, 6, 22. 99. W. Wald, Proceedings of the Polyurethane Foam Association Technical Program, Arlington, VA, USA, May 1998, Paper No.6. 100. G.L.A. Sims and D. Pentrakoon, Cellular Polymers, 1997, 16, 6, 431.

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Flexible Polyurethane Foam 101. G.L.A. Sims and J.A. Bennett, Polymer Engineering and Science, 1998, 38, 1, 134. 102. InTouch, 1996, 5, 2, 2. 103. Polyurethane Foam Association Technical Program Abstracts, May 2000 to October 2002. 104. American Chemistry Council, Responsible Care, http:// www.americanchemistry.com/prodserv.nsf/s?readform&cbes-5hx2vj 105. Code of Federal Regulations Title 40, Parts 9 and 63, Environmental Protection Agency, Washington, DC, USA. 106. P. Conner, Proceedings of the Polyurethane Foam Association Technical Program, Arlington, VA, USA, May 2000, Paper No.2. 107. B. Cummings, Proceedings of the Polyurethane Foam Association Technical Program, Salt Lake City, UT, USA, October 2002, Paper No.6. 108. R. Sack, Proceedings of the Polyurethane Foam Association Technical Program, Salt Lake City, UT, USA, October 2002, Paper No.4. 109. C. Ecob, Proceedings of the Polyurethane Foam Association Technical Program, Salt Lake City, UT, USA, October 2002, Paper No.5. 110. B. Blackwell, Proceedings of UTECH, 2000, The Hague, The Netherlands, Innovations: Flexible Foam Development Session, Paper No.1. 111. R. Milian, Proceedings of the Polyurethane Foam Association Technical Program, New Orleans, LA, USA, October 2001, Paper No.1. 112. J.G. Kniss, L.A. Mercando and M.L. Listemann, Proceedings of the Polyurethane Foam Association Technical Program, Newport, RI, USA, October 2000, Paper No.1. 113. E. Rister, Proceedings of the Polyurethane Foam Association Technical Program, Arlington, VA, USA, May 2002, Paper No.3. 114. S.P. Levine, Proceedings of the Polyurethane Foam Association Technical Program, Arlington, VA, USA, May 2001, Paper No.5. 115. L. Peters, Europur Presentation, Helsingor, Denmark, June 1996, Slides 17 and18. 121

Handbook of Polymer Foams 116. E. Okumus, Arbetarskydd, February 19th, 1999, 6. 117. M. Dalene, G. Skarping and P. Lind, American Industrial Hygiene Association Journal, 1997, 58, 8, 587. 118. K. Hall, F.A.L. van Parys and R.J. Young, Plastics, Rubber and Composites, 2001, 30, 9, 426. 119. K. Hillier, D. King, A. Kronborg-Hansen and T. Schupp, Cellular Polymers, 2001, 20, 4, 279. 120. InTouch, 1997, 6, 2, 2. 121. InTouch, 1994, 4, 1, 3. 122. F. Lichtenberg, Proceedings of the Polyurethane Foam Association Technical Program, May 2002, Arlington, VA, USA, Paper No.2. 123. Sustainability, PURRC Pamphlet, PURRC, New York, NY, USA, 1997. http:// www.utm.edu/~moo/purrc/advanced.html 124. There are a Variety of Ways to Recycle Polyurethane, API Pamphlet, Arlington, VA, USA. http://www.polyurethane.org/polyurethane_recycling/ how_poly_recycled/purrc2.html 125. S.H. Shin, J.H. Chun and B.S. Tae, Proceedings of the SPI Polyurethanes World Congress, Las Vegas, NV, USA, 1996, p.77.

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Rigid PVC Foam

6

Rigid PVC Foam Noreen L. Thomas

6.1 Introduction Rigid polyvinyl chloride (PVC) foam (flexible PVC Foam is covered in Chapter 7 of this book) was first produced some thirty years ago, when it was heralded as ‘the wood of the future’ [1, 2]. Now this material has a well-established market in Western Europe of about 300 ktonnes. The product range covers diverse applications such as window sills, sewer pipes and advertising boards. The reasons for the success of this material are its ability to compete with wood and also the benefits that it offers over solid PVC. Many of the applications for extruded PVC foam profile (in the density range 500 to 800 kg/m3) are for wood-replacement products. It can be sawn, nailed or screwed without splitting or cracking, thus allowing use of woodworking methods. Foamed extrudates can be produced to resemble wood in terms of structure, colour and appearance. Hence rigid PVC foam profile is often used as a direct substitute for wood. This is being driven [3] by environmental pressure to protect forests, the rising price of timber and the advantages of a maintenance-free product. On a cost/volume basis PVC foam is more expensive than wood but becomes more cost effective when wood finishing operations are taken into account. PVC foam can be extruded into complex shapes (some of which are not possible with wood) without the finishing operations and scrap associated with the manufacture of wood trim. In addition PVC foam offers the following advantages over wood [4, 5]: chemical resistance, good weatherability, (i.e., does not rot), good fire retardancy (Class B1, based on DIN 4102 [6]), and resistance to infestation by vermin. The main obstacles to its use are its reduced toughness and higher cost compared with wood. Apart from its success as a replacement for wood, rigid PVC foam is also being used to replace solid PVC. This is because foamed PVC provides a number of advantages over the solid polymer. Firstly, foaming gives a lower cost per unit volume of product, which in today’s highly competitive and cost conscious environment is a very important consideration. The economics of extruding foamed versus solid PVC are examined by

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Handbook of Polymer Foams Patterson and Hughes [7] and also by Dobrowsky [8]. Other benefits of foaming [4, 9] are lower thermal conductivity (hence improved insulation), reduced thermal expansion, improved acoustic damping properties, higher stiffness (due to increased cross-sectional area for a given weight) and improved resistance to wind-load. There are three major markets for rigid PVC foam: profile, sheet and pipe. Within Western Europe the current sizes of these sectors are estimated to be 60, 50 and 180 ktonnes, respectively. These markets are regional, reflecting the disparate preferences in building design and differences in building regulations throughout Europe. For example, the UK is by far the largest market for foam profile, whereas foam sheet is predominantly produced in Germany, with additional production in Switzerland, UK and Eire. The most important market for foam pipe has always been France, although now significant quantities are also manufactured and used in Germany, the Netherlands and Spain, with some production in Switzerland and the UK. As discussed previously, rigid PVC foam profile is mainly produced for wood-replacement products [5]. These are used in both weathering (exterior) and non-weathering (interior) applications. Examples of weathering applications include cladding, soffit boards, roofing products, windowsills and door-frames. Examples of non-weathering applications are skirting boards, cornices, wall and ceiling panelling, curtain rails, guide rails for shutters, coving and furniture profiles. PVC foam sheet is used in a variety of applications [5, 10] including display panels, signs, advertising boards, partition panels, building panels, garage door panels, table tops and shelves. It is used as the core material of sandwich structures in boat building, and for tanks and refrigerated vehicle bodies. PVC foam sheet is suitable for printing, painting and silk-screening. Sheets can be thermoformed, even after printing, and this opens up an even wider range of possible applications. Foam core pipe is used in applications in which there is no internal pressure [5, 11]. Products include drain pipes, sewer pipes, effluent discharge pipes, ventilation ducts, cable conduits and winding cores for textiles and paper. Apart from its considerable market share in Europe, it also enjoys widespread use in other countries, such as the USA, Australia and China [8].

6.2 Foam Extrusion The principal method for the production of PVC foam profile, sheet and pipe is extrusion. The cellular structure is generated by the decomposition of chemical blowing agents (CBA), which are organic or inorganic compounds that decompose on heating to evolve

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Rigid PVC Foam one or more gases. Physical blowing agents (PBA), which are gases or low boiling point liquids, are not widely used in the production of rigid PVC foam.

6.2.1 Basic Principles The basic principles for the extrusion of polymer foams were first elucidated by Hansen [12, 13] and have also been discussed by Han [14] and Gale [15]. Gas is introduced into the molten polymer in the extruder barrel either by thermal decomposition of CBA or by direct injection of PBA. The principles involved are similar for both types of blowing agent because the gaseous decomposition products from the CBA are generated within the extruder barrel and dissolve in the molten polymer. Dissolution is possible because of the high melt pressure within the extruder. To achieve an optimum foaming operation it is essential that bubble nucleation is delayed until the polymer melt emerges from the die. Hence high pressure must be maintained throughout the barrel and die to keep the gas in solution. This requires appropriate screw and die design, as well as good temperature control. By lowering the die temperature both melt viscosity and pressure are raised, and this will suppress any undesirable, premature foaming. When the melt exits the die, the rapid drop in pressure causes the polymer to become supersaturated with gas. Phase separation occurs and almost instantaneous nucleation of bubbles takes place. Bubbles will nucleate at irregularities in the polymer melt such as CBA solid residues, pigments, fillers, etc. The growth rate of the bubbles is rapid at first and then decreases as the pressure within them diminishes. Bubble growth is also retarded as the polymer cools down and its viscosity increases. To prevent the foam structure from collapsing, it is essential to cool the material very rapidly. This is done by passing the foam through a chilled calibration unit so that the cellular structure is rapidly ‘frozen’ into place. The surface quality, density and thickness of the outer skin are all influenced by the distance between the die and the calibration unit as well as the intensity of the cooling. Many aspects of the foam morphology are controlled by the formulation used. These are discussed in detail in Section 6.3. Cell size and uniformity depend critically on the amount and type of chemical blowing agent. A uniform, closed, fine cell structure is desirable for most applications. Cell size is also a function of the rheological properties of the polymer. If the polymer viscosity is too high, then the bubbles will not be able to expand fully, and it will not be possible to achieve a low density foam. If the polymer viscosity and melt strength are too low, the cells will rupture and/or collapse. In the case of PVC, melt strength is determined by the molecular weight of the polymer and by the use of acrylic processing aids.

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6.2.2 Extrusion Processes Rigid PVC foam is processed from dry blend on parallel or conical, contra-rotating, twin-screw extruders. These are basically the same machines as used for producing solid product with some differences in screw design [5]. The big difference in foam extrusion is in the die and calibration systems used. There are essentially two methods of foaming [5, 9, 11, 16], described as the free-foaming and Celuka methods. The free-foaming method is illustrated in Figure 6.1. The polymer melt is allowed to expand freely after exiting the die, prior to entering the calibration system, which is situated a short distance away. The extrudate has an even foam density distribution across its thickness and a thin higher density skin (Figure 6.2). This process can be used to produce pipe, sheet and simple profiles. The free-foam method is the preferred process for the extrusion of rigid PVC foam sheet [17]. Product thicknesses can be obtained between 2 and 20 mm and widths from 1 to 2 metres. Typical throughput rates are in the range 200 to 600 kg/h. Special temperature controlled die lips can be used to give different processing temperatures for the upper and lower lips of the die. A 3-roll polishing stack is used for calibration and cooling. The free-foam process offers several advantages over the Celuka method for sheet extrusion. The lines are more flexible and do not require new dies and calibrator modifications every time that the sheet thickness is changed. This gives a simpler production process with less investment cost. Figure 6.3 is a scanning electron micrograph of a cross-section through the thickness of a sample of PVC foam sheet made by the free-foam process. This foam has an average density of 600 kg/m3 and shows a fine, even, closed cell morphology.

Figure 6.1 Schematic diagram of free-foaming method Redrawn with permission from G. Beckmann, Proceedings of the PRI PVC ’87 Conference, Brighton, UK, 1987, Paper No.13, Figure 1. Copyright 1987, Institute of Materials

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Figure 6.2 Density distribution across thickness of free-foam product Redrawn with permission from G. Beckmann, Proceedings of the PRI PVC ’87 Conference, Brighton, UK, 1987, Paper No.13, Figure 3. Copyright 1987, Institute of Materials

Figure 6.3 Scanning electron micrograph of cross-section through free-foam sheet

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Handbook of Polymer Foams The Celuka process is also known as the inward-foaming method. The calibration unit is situated adjacent to the die and has the same dimensions as the die, thus controlling foam expansion. This set-up gives very rapid cooling. Bubble formation is quenched in the surface of the product and a solid outer skin is produced. The die contains a mandrel [18], which controls melt pressure decay and allows the melt to foam freely inside the profile (Figure 6.4). The density distribution across the thickness of the Celuka foam profile (see Figure 6.5) is quite different from that produced from the free-foaming process. There is a solid outer skin, usually about 0.5 mm thick, and a lower density core. The outer surfaces of Celuka products are the same as those of solid extrusions, whereas free-foam products have a rougher, more textured surface finish. The Celuka method is used for making pipes, sheet and profiles of complex geometries. Figure 6.6 is a scanning electron micrograph of a cross-section through a Celuka foam profile. This foam has the same average density as that pictured in Figure 6.3, (i.e., 600 kg/m3) but has a coarser cell structure because of differences in formulation (see Section 6.3). The solid Celuka skin, which is formed by quenching of the melt against the chilled calibrator surface, can be seen on the right hand side of this micrograph. Also to the left of the centre of the picture is a vertical line corresponding to the join between the two melt streams that have been separated by the mandrel in the die. This line lies midway through the thickness of the profile and corresponds to the dip in density shown at the centre of Figure 6.5. It is very important that the two melt streams become properly fused: otherwise a plane of weakness will exist at the centre of the profile.

Figure 6.4 Schematic diagram of Celuka method Redrawn with permission from G. Beckmann, Proceedings of the PRI PVC ’87 Conference, Brighton, UK, 1987, Paper No.13, Figure 2. Copyright 1987, Institute of Materials

128

Rigid PVC Foam

Figure 6.5 Density distribution across thickness of Celuka product Redrawn with permission from G. Beckmann, Proceedings of the PRI PVC ’87 Conference, Brighton, UK, 1987, Paper No.13, Figure 4. Copyright 1987, Institute of Materials

Figure 6.6 Scanning electron micrograph of a cross section through a Celuka profile

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Handbook of Polymer Foams The advantages of the Celuka process are that the solid skin gives a product with a harder surface, better appearance, improved impact properties and higher stiffness. Also this process can be used for making profiles with complex shapes, which would be very difficult by the free-foam method. Another important process, which is now widely used, is co-extrusion of a surface layer of solid PVC over the foamed product. This can be used to produce harder, glossier surfaces or different colours. It also has the advantage that unpigmented and/or recycled material can be used in the foamed core. The co-extruder, which can be single or twinscrew, feeds material to form the compact outer skin to an outer die with the same shape as the desired profile [5]. Co-extrusion can be used in conjunction with either Celuka or free-foam processes. An example of a profile produced by co-extruding a skin over a Celuka foam profile is illustrated schematically in Figure 6.7. This is co-extruded foam cladding with a skin covering the top surface. Obviously the co-extruded skin is only required on the surface exposed when the product is in use. Figure 6.8 is a scanning electron micrograph showing a cross-section through co-extruded foam profile, which has an overall density of 500 kg/m3. In the production of foam core pipe, co-extrusion is used to produce the solid skin on both exterior and interior surfaces [8, 19]. Either one or two co-extruders may be used [20, 21]. When only one co-extruder is used, the gelled skin material is fed into the die where it is divided into two concentric layers between which the core material is supplied [21, 22]. Other systems involve the use of two co-extruders to feed inner and outer skins [21]. Proponents of the latter, while acknowledging the additional capital outlay required, claim that there is better control over outer and inner skin thicknesses and improved weld line strength between the layers [20, 21]. No special downstream equipment is

Figure 6.7 Schematic diagram of co-extruded foam cladding

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Rigid PVC Foam

Figure 6.8 Scanning electron micrograph of a section through a co-extruded foam profile

required, but because foam core pipe is a better thermal insulator than solid PVC (and is therefore harder to cool), it may be necessary to install longer water tanks than those normally used for cooling solid PVC pipes.

6.2.3 Effect of Processing Conditions The choice of processing conditions plays a critical role in determining foam morphology and density - and hence the physical and mechanical properties of the product. The heat and shear imparted to the material will determine the rate of decomposition of the blowing agent, melt viscosity of the polymer and the degree of gelation of the polymer. Kim and co-workers [23] have shown that foam density generally decreases with increasing extrusion temperature up to a certain optimum temperature and thereafter begins to rise. Similar observations have been made by Rabinovitch and co-workers [24]. The explanation is that at low temperatures the foaming process is inefficient because of high polymer melt viscosity coupled with low gas pressure. Foaming efficiency improves with increasing temperature but above the optimum temperature range density begins to rise because too low a melt viscosity causes cell rupture and collapse.

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Handbook of Polymer Foams The effect of volumetric flow rate has also been studied by Kim and co-workers [23], who found that foam density decreased with increasing extrusion rate. This was attributed to better mixing and reduced viscosity. Thomas and co-workers [25] have also investigated how foam density is affected by extrusion screw speed. They reported that foam density decreased by 24% as the screw speed was increased from 6 to 14 rpm and thereafter remained constant (see Figure 6.9). At the highest screw speed investigated (18 rpm) there was evidence of cell collapse and so an intermediate screw speed was recommended. Rabinovitch and co-workers [24] also found that for very high screw speeds there is a substantial increase in foam density due to cell collapse and attributed this to shear heating. Brenis [26] investigated a number of processing variables and concluded that the most influential in controlling foam density were the front cylinder zone temperatures, screw temperature and screw speed. Other variables such as adapter, flange and die temperatures had less effect on density but were more influential over surface finish: running with these temperatures lower produced a smoother surface skin. Work by Thomas and coworkers [25] has also confirmed that the front barrel zone temperatures have the greatest effect on foam density.

Figure 6.9 Effect of screw speed on foam density [25]

6.3 Foam Formulation Technology As in all PVC applications, the formulations for the production of foamed PVC are a complex mixture of thermal stabilisers, lubricants, processing aid, pigment and filler, in addition to the blowing agents required to produce the cellular structure. The type of

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Rigid PVC Foam PVC and formulation ingredients control the thermal stability, gelation behaviour, powder flow characteristics, melt viscosity and melt strength of the material during the production process. Hence all the components of the formulation will influence the subsequent foam density, surface finish and overall properties of the foam [3] and there may be interactions between individual ingredients.

6.3.1 Blowing Agents

6.3.1.1 Chemical Blowing Agents There are many criteria for the choice of a suitable chemical blowing agent [27]. Obviously it is essential that decomposition takes place within the processing temperature range of the polymer. In the case of rigid PVC foam, this processing window is between 160 °C and 190 °C. The blowing agent should not decompose too quickly, but should have a high gas yield and be economical to use. It requires good long-term storage stability and ease of incorporation and dispersion in the polymer. It should have the ability to produce a fine, even cell structure and a stable foam that is not prone to collapse. The decomposition products should be compatible with the polymer and not have an adverse effect on its processing characteristics or thermal stability. Furthermore, both the blowing agent and its decomposition products should be non-toxic and ‘environmentally friendly’. Unfortunately there is no perfect candidate that can meet all these requirements. The blowing agents most commonly used in the production of rigid PVC foam are azodicarbonamide (ADC) and sodium bicarbonate (SBC), and they are often used together because of synergism. ADC is widely used in the plastics industry, particularly in the production of PVC plastisol foams. It has the structure H2N-CO-N=N-CO-NH2 and decomposes exothermically at about 215 °C to give a gas yield of 220 cm3 [5]. The major gaseous decomposition product is nitrogen, which constitutes about 60% by volume of the gases evolved. Other gaseous products are CO2, CO and NH3. The relative amounts of these depends on the decomposition mechanism of ADC, which varies as a function of environmental factors, such as pH [27, 28, 29]. Although the decomposition temperature of ADC lies outside the processing window of rigid PVC foam, there are numerous activators or kickers [30] that can lower the decomposition temperature into the required range. Some examples of these are zinc and lead salts, which are also added as thermal stabilisers for PVC [29, 31]. A blowing agent that is sometimes mixed with ADC to act as a kicker is oxybisbenzenesulfonyl hydrazide (OBSH) [32]. It decomposes in the temperature range 150 to 160 °C and evolves nitrogen and water vapour. The extent to which the decomposition temperature of ADC is reduced depends on the ratio of ADC to OBSH in

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Handbook of Polymer Foams the mixture. Work is still underway to find new kickers for ADC and thereby obtain better control of the foaming process [33]. One of the main advantages of using ADC is that it is a very efficient blowing agent. This is illustrated in Figure 6.10 [34], which shows how the foam density of an extruded freefoam strip varies with the concentration of ADC in the formulation. There is a sharp decrease in density from 1400 to 500 kg/m3 as the ADC level is increased from zero to about 0.5 parts per hundred parts of PVC (phr). The density then stays constant and eventually begins to rise as the ADC concentration is further increased. The explanation for this phenomenon is that with increasing levels of blowing agent above an optimum amount the cells begin to collapse and coalesce [3, 35]. In summary, ADC is a highly efficient exothermic blowing agent, which gives a high rate of gas expansion and a fine, uniform cell structure [34, 36] - as illustrated in Figure 6.3. Its disadvantages are that it can cause cell collapse if used in too high a concentration and may give yellowish foams. Also it is classed as an irritant and may cause allergic respiratory reactions. SBC is a well-known blowing agent because of its use in baking powder. Its decomposition is endothermic and reversible and takes place over a wide temperature range, which fortunately coincides with the processing window for rigid PVC foam. The decomposition

Figure 6.10 Effect of ADC concentration on foam density [34]

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Rigid PVC Foam products are CO2, H2O and Na2CO3 and the gas yield is 125 cm3. Compared with ADC, its decomposition has been described as slow and erratic [36]. SBC is a less efficient blowing agent than ADC. The effect of increasing levels of SBC on the density of extruded free-foam strip was investigated [34] and the results are shown in Figure 6.11. There is an almost linear relationship between increasing SBC concentration and decreasing foam density: cell collapse was not detected in these experiments. To produce a foam with a density of 500 kg/m3 it was necessary to use 2 phr of SBC, compared with 0.5 phr of ADC (Figure 6.10). Also the foams produced using SBC had a coarse, irregular cell structure [34, 37]. In summary, SBC decomposes over a wide temperature range, the reaction does not go to completion and the gas yield and pressure are relatively low compared with those of ADC. The cell structure tends to be coarse and irregular, which can lead to inferior impact properties (see Section 6.4). However, previous problems of variable gas yields and poor dispersion, caused by the hygroscopic nature of SBC, have largely been overcome with current products, which are coated with oil or wax [30]. The advantages of SBC are that it is easier to handle than ADC, produces a whiter foam and is less prone to give problems with cell collapse.

Figure 6.11 Effect of SBC concentration on foam density [34]

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Handbook of Polymer Foams Bearing in mind the complementary properties of the two blowing agents, it is not surprising to find synergistic effects when they are used together. Combined use of ADC and SBC has been reported to give better control of extrudate density, product colour and processability [36]. Overall it is possible to obtain a lower density foam which is less prone to cell collapse. This is illustrated in Figure 6.12, which shows a 3-D plot of foam density as a function of the levels of ADC and SBC in the formulation. It can be seen that the lowest density foams are produced using a combination of the two blowing agents. Another advantage of using a combination of ADC and SBC is that a finer cell structure is achieved than can be obtained with SBC alone [38]. It seems that nitrogen produced from the decomposition of ADC readily nucleates bubbles and these act as nucleation sites for CO2 bubbles from the decomposition of SBC. The propensity for nitrogen bubbles to form more readily than carbon dioxide may be explained by the fact that the solubility of nitrogen in PVC is 20 times lower than that of carbon dioxide [39]. The optimum ratio of ADC:SBC depends on the application and the processing method used [40]. For rigid PVC profiles, which are generally produced by the Celuka process, a high level of SBC is used with a low level of ADC, which acts as a ‘nucleating agent’ to ensure a reasonably fine cell structure. Foam sheet is largely produced by the free-foam process and here it is found that formulations with a high concentration of SBC give a poor surface finish. Hence the best systems for this application are mixtures of exothermic blowing agents either without SBC or with a low level. Similarly for foam core pipe the blowing agent is mainly exothermic with a small amount of SBC, if any.

Figure 6.12 Effect of combined use of ADC and SBC on foam density [34]

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Rigid PVC Foam

6.3.1.2 Physical Blowing Agents Physical blowing agents are rarely used in the extrusion of foamed PVC. However, the question arises as to why not use direct gassing of carbon dioxide and nitrogen to replace chemical blowing agents: these gases are said to be a factor of ten cheaper when used from cylinders than when obtained from CBA [15]. In fact there was a widespread attempt to use CO2 in thermoplastic foam extrusion [41], but it is difficult to get the same product quality as achieved with other blowing agents both in terms of surface finish and foam consistency. There are problems in delivering the gas to the extruder and sealing the extruder to prevent gas leaking back through the hopper. Nitrogen gas is also used as a blowing agent, but to a lesser extent than carbon dioxide: it is said to be more difficult to work with than CO2. However, in the longer term, the use of inert gases may be the way forward for physical blowing agents in foam extrusion. Gale [15] has described experiments using carbon dioxide, nitrogen and argon as blowing agents for foam extrusion. Carbon dioxide was found to give the best results and was used in further trials of both commodity and engineering polymers [42]. A standard extruder was used with retrofitted parts, including a cavity transfer mixer to mix the CO2 as a supercritical fluid into the polymer melt. The experiments were successful and it was concluded that the commercialisation of direct gas injection of CO2 may depend on capital costs and plant responsibilities for handling high pressure gas as much as any other technical issue. In terms of PVC extrusion, Dey and co-workers [43] have reported a novel method of extruding high density, rigid PVC foam using a commercial PVC compound with inert gas PBA (CO2 or argon). The process was developed on a segmented single screw extruder with L/D ratio of 40. Gas was injected into the barrel through a nozzle in a Dynisco type port. An electronic gas-pressure controller was used to regulate the gas injection pressure, and the mass flow rate of the blowing agent was monitored with a Matheson gas flow meter. Using this set-up they were able to produce free foam rods with densities of the same order as currently produced by conventional technology using chemical blowing agents. It was difficult to get a fine foam structure with CO2 but there was an improvement when talc was added as a nucleating agent. Direct gas injection of CO2 and N2 is also being used in the emerging technology of microcellular foam extrusion [44, 45] - see Section 6.5.2.

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6.3.2 Processing Aids Processing aids, based on acrylic copolymers of relatively high molecular weight, are widely used in PVC extrusion processes to promote fusion, enhance surface finish, and increase melt extensibility and strength [46, 47]. In formulations for rigid PVC foam there is no doubt that processing aid is a key ingredient [10, 48, 49]: the improvement conferred in both melt elasticity and strength prevents collapse of the cellular structure. The importance of the molecular weight of the processing aid was first demonstrated by the work of Ide and Okano [50]. They showed that the tendency for foam density to increase at high concentrations of blowing agent was arrested if a high molecular weight processing aid was used. With increasing molecular weight, it was possible to achieve progressively lower foam densities before cell collapse took place. This result was confirmed by Pfennig and Ross [35]. Choice of higher molecular weight processing aid also gives foams with improved surface appearance [47]. The effect of processing aid concentration on foam density has been examined by Szamborski and Pfennig [10]. They found that for both tin and lead stabilised PVC foam sheet formulations, increasing the concentration of processing aid up to 8 phr gave significant density reductions. Surface finish was also improved. The influences of both concentration and molecular weight of processing aid on the density of extruded free-foam strip are shown in Figure 6.13 [51]. It can be seen that for all processing aids there is a reduction in foam density as the addition level is increased from 4 to 8 phr, although the effect is less evident at high molecular weights. The corollary is that a desired improvement in melt strength may be achieved either by use of high molecular weight or by high level of processing aid. Measurements carried out using an elongational rheometer have confirmed that melt extensibility and rupture stress are increased with increasing addition level and/or molecular weight of processing aid [51]. The important relationship between processing aid and blowing agent, established by the work of Ide and Okano [50] and Pfennig and Ross [35], is a key factor in the formulation technology of PVC foam. It is important to get the right balance between these ingredients to avoid cell collapse on the one hand and unnecessary use of too much processing aid on the other. This relationship is illustrated in the 2-D contour plot of Figure 6.14 [34], which shows foam density as a function of the level of both blowing agent and processing aid. At processing aid levels of 3 phr and below, the lines of constant foam density run parallel to the blowing agent axis. Hence, increasing blowing agent has no effect on foam density because cell collapse takes place. However, in the bottom right

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Rigid PVC Foam

Figure 6.13 Effect of processing aid molecular weight and level on foam density [51]

Figure 6.14 Two dimensional contour plot showing effect of concentration of blowing agent and processing aid on foam density [34]

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Handbook of Polymer Foams hand corner of the plot the lines of constant foam density run parallel to the processing aid axis, showing that density reduction cannot be achieved with high levels of processing aid if there is insufficient blowing agent.

6.3.3 Type of PVC The molecular weight of PVC is usually expressed in terms of K-value, which is a measure of the solution viscosity of the polymer. This is the most important parameter determining the suitability of PVC for foam extrusion. Too low a K-value gives a low melt strength, so that the foam will easily rupture and/or collapse. Too high a K-value gives a highly viscous melt, so that bubbles are unable to expand fully. In both cases the result is a high density foam. Patterson and Szamborski [3] have examined the effect of PVC K-value on foam density. They compared resins of K-values 51, 57, 60, 66 and 68, and found that the lowest foam densities were produced with K57 and K60 resins. It is generally recognised that the best PVC for rigid foam is suspension or mass polymer with a K-value in the range K56 - K62. Higher K-value resins (in the range K65 to K68) are sometimes used for the production of foam core pipe [8]. In this case, melt extensibility is improved by the use of processing aid.

6.3.4 Stabilisers Stabilisers perform a dual role in PVC foam formulations: they prevent thermal degradation of the polymer and function as activators for the decomposition of ADC [29, 30, 31]. Lead and zinc stearates are particularly effective in the latter respect. Lead stabilisers are widely used in foam formulations in Western Europe for both profiles and pipes. They are relatively cheap, have a lubricating effect and give a wide processing window. Calcium/zinc formulations have a small share of the foam profile market. They offer advantages over lead because of their lower toxicity, but they are more expensive and provide a smaller processing window. Organotin stabilisers can be divided into two types: mercaptides and carboxylates. The majority of tin stabilisers used are mercaptides. They are excellent heat stabilisers but give poor weatherability and do not have a kicking action on ADC. Hence formulations based on tin mercaptide, which are used for the majority of non-weathering foam sheet products, require ‘kickers’ for ADC decomposition: otherwise a low gas yield will result [3, 9, 31].

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Rigid PVC Foam Tin carboxylates are more expensive than tin mercaptides but offer excellent weathering properties and do act as ‘kickers’ for ADC decomposition [52]. These stabilisers are a good choice for free-foam sheets for outdoor applications, (e.g., advertising boards or garage door panels).

6.3.5 Lubricants Lubricants are essential ingredients in any PVC formulation because of their role in controlling gelation, melt viscosity, flow and surface finish. In the foaming process it is important that the PVC blend gels early enough in the extruder so that gaseous decomposition products from the CBA can dissolve in the melt and are not drawn off in the vent or even lost back up the hopper. Also it is essential to generate enough shear to decompose the blowing agent. However, too much shear heating will cause cell collapse. Hence a balance of internal (compatible) and external (incompatible) lubricants is required [5, 9]. Decker [53] has demonstrated that the type of lubricant not only affects the ease of processing, but also determines the effectiveness of the blowing agent and hence the final density of the product.

6.3.6 Typical Formulations The majority of the rigid PVC foam profile produced in Western Europe is lead-stabilised and a typical formulation is given in Table 6.1 [25]. This formulation serves as a guide: it requires tailoring for the particular extruder and product in question. Levels and/or

Table 6.1 Guideline lead-stabilised formulation for rigid PVC foam profile [25] Ingredient

Parts per hundred parts of polymer (phr)

PVC resin - K57

100

Lead stabiliser

3-4

Lead co-stabiliser and lubricant

0.4-0.6

Lubricants (internal and external)

1.0-2.0

Acrylic processing aid Blowing agent (SBC and ADC)

5-8 1.5-2.5

Titanium dioxide pigment

1-5

Filler (calcium carbonate)

4-8

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Handbook of Polymer Foams type of stabiliser, pigment and filler should be adjusted depending on whether the foam is co-extruded and whether the product is intended for outdoor use. Table 6.2 shows a typical formulation for PVC free-foam sheet [5, 10, 49]. The same considerations as discussed previously apply in terms of adjustment of the formulation to the process and product. In particular, the choice of tin stabiliser as well as the level and type of pigment should be governed by the weathering properties required of the finished product. A typical formulation for foam core pipe is given in Table 6.3 [5, 8]. To reduce costs, the maximum amount of filler and minimum amount of processing aid are used commensurate with the properties required in the final product.

Table 6.2 Guideline tin-stabilised formulation for rigid PVC foam sheet Ingredient PVC - resin (K57 - K60)

Parts per hundred parts of polymer (phr) 100

Tin stabiliser

1.0-2.0

Epoxy compound (co-stabiliser)

1.0-2.0

Lubricants (internal and external)

1.5-2.5

Acrylic processing aid

6-10

Blowing agent (ADC)

0.4-0.8

Titanium dioxide pigment

1-5

Filler (calcium carbonate)

4-8

Table 6.3 Guideline lead-stabilised formulation for PVC foam core pipe Ingredient

Parts per hundred parts of polymer (phr)

PVC - resin (K65 - K68)

10 0

Lead stabiliser and co-stabiliser

2-3

Lubricants (internal and external) Processing aid Blowing agent (ADC) Filler (calcium carbonate)

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0.8-1.5 3-6 0.5-0.7 5-12

Rigid PVC Foam

6.4 Properties The rapid growth in the market for rigid PVC foam products in recent years has been due to the benefits that these materials offer over both wood and solid PVC. Some obvious advantages of foamed PVC over wood are good weatherability, improved chemical resistance, good fire retardancy and excellent resistance to attack by vermin [4, 5]. Over solid PVC, the advantages of foaming are a lower cost per unit volume of product, higher stiffness for the same weight of material, better acoustic damping properties, improved resistance to wind load, lower thermal conductivity and lower thermal expansion [7, 8, 9]. A comparison of the thermal expansion and thermal conductivity coefficients of PVC foam versus solid PVC are given in Table 6.4, showing the reduction produced on foaming. Also included in Table 6.4 is a comparison of the mechanical properties of foamed and solid unplasticised (PVC-U), together with the test methods used for their measurement. It is found that, in common with all other materials, the mechanical properties of the foamed products are reduced in comparison with their solid counterparts. However, it is clear that the method of foaming influences the properties of the material produced. For example, although the Celuka profile has a lower density than the free-foam board, it has a considerably higher impact strength and hardness, due to the integral skin generated in the Celuka process. The characteristics of a foam that determine its mechanical properties [62] are: foam density (including density distribution through the product thickness), skin integrity and thickness, surface texture, and cell morphology, (i.e., cell size and uniformity). However, according to studies of a large number of different polymer foams over a wide range of densities [63], the single most important factor controlling the mechanical properties of foamed materials is the relative density (Ø), i.e., the ratio of the average foam density to the density of the solid material. Throne [64] has reported results of mechanical properties of a number of thermoplastic structural foams (which did not include PVC) over a relative density range of 1.0 to 0.5. Many properties, such as tensile strength, compressive modulus, shear modulus, fatigue strength and creep strength, were found to obey an empirical square law relationship with relative foam density as expressed by the equation: X = Xo.Ø2

(6.1)

where X is the mechanical property of the foamed product and Xo is the mechanical property of the unfoamed material. Young’s modulus of thermoplastic foams [62] has also been shown to depend on the square of the relative density (Equation 6.1).

143

144

Vicat softening temperature

Modulus of elasticity DIN EN ISO 306 [61]

ISO 178 [60]

1,200 63

°C

50

40

16

17.5

12

MPa

-

DIN 53505 [59]

MPa

Shore D hardness

DIN EN ISO 527-1 and 527-2 [57, 58]

Tensile stress at break

MPa

%

DIN EN ISO 527-1 and 527-2 [57, 58]

Tensile stress at yield

kJ/m2

0.062

0.50 x 10-4

K-1 W/mK

600

Free foam profile 120 x 3 mm kg/m3

Units

Elongation to break

DIN EN ISO 179 [56]

DIN 52612 [55]

VDE 0304

DIN 53420 [54]

Test method

Impact strength @ 23 °C

Thermal conductivity

Coefficient of linear thermal expansion @ 20 °C

Density @ 23 °C

Property

67

1,200

80

30

15

17

25

0.062

0.54 x 10-4

550

Celuka profile 140 x 10 mm skin = 0.5 mm

Values

78

3,050

80

27.5

35

58

no failure

0.16

0.70 x 10-4

1,400

Solid

Table 6.4 Comparison of properties of foamed and solid PVC (Reproduced from [16] with permission)

Foamed Solid PVC

Handbook of Polymer Foams

Rigid PVC Foam Flexural properties [64] were found to fit the expression: X = Xo.Ø3/2

(6.2)

or for samples with carefully controlled skin thicknesses and high foam density the linear law of mixtures gave the best fit, as shown in Equation 6.3. X = Xo.Ø

(6.3)

Data [11, 16, 65] for the mechanical properties of rigid PVC foams do not appear to follow the square law relationship. Tensile strength data more nearly fit a law of mixtures (Equation 6.3), whereas flexural properties gave a better fit to Equation 6.2. Yield stress and Young’s modulus data fall somewhere between the values predicted from Equations 6.2 and 6.3, presumably depending on other morphological features in addition to average foam density. For example, density distribution and skin thickness are particularly important in determining flexural properties, Young’s modulus and creep behaviour [62]. Impact behaviour is an important feature of rigid PVC foams. However, there appears to be no theoretical or empirical relationship to describe adequately the impact characteristics of thermoplastic structural foams. The main factors affecting impact properties are overall thickness, foam density and skin thickness [62]. The solid skin is important to eliminate crack-initiation caused by bubbles acting as stress raisers in the surface. A fine, even cell structure will improve impact properties. With this type of foam morphology, surface texture is minimised and the risk of crack initiation from coarse bubbles at the surface is reduced: where crack propagation does occur, it will be much more localised. Hence the method of fabrication and choice of blowing agent level and type are all key factors in determining the impact strength of the foamed product.

6.5 Novel Processes and Applications

6.5.1 Recycling PVC has been the subject of much environmental debate and scrutiny over recent decades, covering many aspects of its lifecycle. One particular criticism is that PVC cannot be recycled. However, this is not the case: PVC is a thermoplastic polymer and like other thermoplastics it can be reground and reprocessed into new products. One of the advantages of producing co-extruded foam profile or pipe is the opportunity that it provides to use recycled material in the foamed core. The recyclate may be industrial

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Handbook of Polymer Foams scrap recovered from pipe production [7] or foam production processes, or it may be material recovered after consumer use. There have been a number of initiatives to use post-consumer PVC recyclate in co-extruded foamed products [66]. For example, in 1990 the PVC pipe manufacturers in the Netherlands, under the auspices of the FKS (the Dutch Federation of Plastic Pipe System Manufacturers), addressed the problem of collecting and using waste PVC pipes and fittings [67]. These materials are now used in the co-extrusion of non-pressure sewage pipe. The skin layers are of virgin PVC and the middle layer consists of recycled material from the collected waste. The middle layer may be compact or foamed depending on the end-use of the pipe. Another successful initiative has been the collection of PVC bottles in France for use in the foamed core of three-layer pipe [68]. It has also been demonstrated that recycled PVC packaging is suitable for use as the foamed core in co-extruded cellular profiles [69, 70].

6.5.2 Microcellular Foam Microcellular foams are dealt with in detail in Chapter 10 of this book. Development of this technology with respect to rigid PVC is discussed below. Microcellular foams are a novel type of thermoplastic foam with an average cell size of about 10 μm. Relative densities can vary from 0.1 to 0.95 and the bubble density from 108 to 1011 bubbles per cm3 [71]. The concept of microcellular foams was devised by Suh of the Massachusetts Institute of Technology in the early 1980s [72] with a view to reducing material costs of mass produced plastic items. The idea was that if bubbles with a smaller diameter than the critical flaws already present in the polymer could be introduced in sufficient numbers, it would be possible to reduce the density without sacrificing mechanical properties. These novel materials were believed to have the potential to revolutionise the way that thermoplastics are used. The key feature about microcellular foams is that homogeneous nucleation is required to produce the very large number of small cells. Homogeneous nucleation will occur when there is a large thermodynamic instability due to a sudden drop in gas solubility: this is induced by creating a rapid pressure drop during processing [73]. Commercial production of microcellular foams is now underway. The technology is known as the MuCell process and is available for both injection moulding and extrusion [74, 75]. The gas is delivered to the system in the form of a supercritical fluid. The process consists of essentially three stages: (i)

Production of a polymer/supercritical fluid mixture,

(ii)

Formation of a single phase polymer/supercritical fluid solution, and

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Rigid PVC Foam (iii)

Inducement of thermodynamic instability to produce homogeneous nucleation and hence a foamed material with a large number of micro-voids.

The MuCell process for PVC [44] has been successfully demonstrated on a variety of different extruders: single screw, counter-rotating twin screw and a tandem arrangement in which a counter-rotating twin screw feeds a single screw extruder. At present all the extrusion applications under development have very low wall thicknesses. High output extrusion processes producing profiles of small cross-sectional area are preferred because under these conditions there is a large pressure drop at the die exit, which is an essential criterion to achieve the very small cell size. Standard PVC formulations can be run [44, 45, 76], although some adjustment to the lubrication is necessary to improve the gloss.

6.5.3 Foamed Composites Linear and crosslinked low density PVC foams are used as core materials in composite sandwich structures [77, 78]. These composites are made for applications such as the hulls of catamarans and door assembly units for recreational vehicles. The structure must be optimised for stiffness, strength, weight and cost. The properties that dominate the choice of the foamed core are shear strength and shear modulus. Compressive strength is also important. Although crosslinked PVC has better mechanical properties than linear PVC for a given density, linear PVC foam has excellent thermoforming properties and is the preferred material for fabrication into complex shapes.

6.6 Summary There is growing demand for rigid PVC foam in both Europe and the USA in the three market sectors of profile, sheet and foam core pipe. Many of the applications for PVC foam profile are for wood-replacement products because of its ease of fabrication and the advantages of a maintenance-free product. Foam core pipe is taking a growing share of the non-pressure pipe market because of its cost effectiveness, higher stiffness for a given weight and facility for the incorporation of recycled material. In order to make a product with the minimum weight for the required stiffness, strength and impact performance, it is necessary to control several aspects of the foam morphology. The most significant properties are foam density and skin thickness, although cell size distribution and surface finish are also influential. The means of controlling these factors are threefold. Firstly, there is the choice of processing method, which can be either free-foam or Celuka with the option of co-extrusion. Secondly, the processing conditions play an important role in determining foam morphology and density. The third element is the formulation.

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Handbook of Polymer Foams Perhaps more so than for other thermoplastic structural foams, there is a complex formulation technology involved in the production of rigid PVC foam products. Formulations contain a mixture of processing aid, thermal stabilisers, lubricants, pigment and filler in addition to the blowing agents required to produce the foamed structure. The type of PVC and other ingredients in the formulation control the powder flow, gelation behaviour, thermal stability, melt rheology and melt strength of the material during the production process, and have an important effect on the properties of the end-product. The formulation and process technology of rigid PVC foam have been well researched. These materials offer the attraction of providing optimum stiffness and strength for the minimum weight of material. Hence, there is a constant drive towards novel applications for PVC foam and also towards new ways of foaming solid products to improve cost effectiveness.

References 1.

R.J. Nightingale, Europlastics Monthly, 1974, 47, 14.

2.

Plastics, Rubber and Textiles, 1970, 1, 485.

3.

J. Patterson and G. Szamborski, Journal of Vinyl and Additive Technology, 1995, 1, 148.

4.

E.C. Szamborski and T.E. Buterbaugh, Plastics in Building Construction, 1993, 18, 7.

5.

H.P. Schneider in Plastics Extrusion Technology, 2nd Edition, Ed., F. Hensen, Hanser Publishers, Munich, Germany, 1997, Chapter 13, 435.

6.

DIN 4102, Fire Behaviour of Building Materials and Components.

7.

J. Patterson and R. Hughes, Proceedings of Vinyl Retec ‘97: Plastic Systems for the Building Industry, Atlanta, GA, USA, 1997, 91.

8.

J. Dobrowsky, Kunststoffe Plast Europe, 1998, 88, 5, 15.

9.

P.S. Schipper, J. Black and T. Dymek, Journal of Vinyl and Additive Technology, 1996, 2, 304.

10. G. Szamborski and J-L. Pfennig, Journal of Vinyl Technology, 1992, 14, 105.

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Rigid PVC Foam 11. R. Brathun and P. Zingsheim in Handbook of Polymeric Foams and Foam Technology, Eds., D. Klempner and K.C. Frisch, Hanser Publishers, Munich, Germany, 1991, Chapter 10, 243. 12. R.H. Hansen and W.M. Martin, Journal of Polymer Science, Part B, 1965, 3, 325. 13. R.H. Hansen, SPE Journal, 1962, 18, 77. 14. C.D. Han, Y.W. Kim and K.D. Malhotra, Journal of Applied Polymer Science, 1976, 20, 1583. 15. M. Gale, Proceedings of Blowing Agent Systems: Formulations and Processes, Rapra Technology Ltd., Shrewsbury, UK, 1998, Paper No.6. 16. G. Beckmann, Proceedings of the PRI PVC ’87 Conference, Brighton, UK, 1987, Paper No.13. 17. Plastics News International, March 1998, 8. 18. P.E. Boutillier, inventor; Kuhlmann Ets, assignee; FP 1,498,620, 1967. 19. Plastics News International, March 1998, 16. 20. M. O’Neill, Modern Plastics International, 1997, 27, 1, 54. 21. A. Odell, Jr, Proceedings of Vinyl Retec ’91, Applying 90s Technology to Vinyl, Fort Michell, KY, USA, 1991, 113. 22. M. Doucat, inventor; Societe Generale de Canalisations (SOGECAN), assignee; EP 19564, 1980. 23. B.C. Kim, K.U. Kim and S.I. Hong, Polymer (Korea), 1986, 10, 215. 24. E.B. Rabinovitch, J.D. Isner, J.A. Sidor and D.J. Wiedl, Proceedings of SPE ANTEC ’97, Toronto, Canada, 1997, Volume III, 3554. 25. N.L. Thomas, R.P. Eastup and T. Roberts, Plastics and Rubber and Composites Processing and Applications, 1994, 22, 115. 26. K.L. Brenis, Proceedings of the 32nd SPE Annual Technical Conference, ANTEC ’74, San Francisco, CA, USA, 1974, 692.

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Handbook of Polymer Foams 27. H. Hurnik in Plastics Additives Handbook: Stabilisers, Processing Aids, Plasticisers, Fillers, Reinforcements, Colorants for Thermoplastics, Ed., R. Gächter and H. Müller, Hanser Publishers, Munich, Germany, 1985, 619. 28. R.A. Marshall, Journal of Vinyl Technology, 1991, 13, 144. 29. R.J. Shute, Proceedings of SPE RETEC PVC Primer, Atlanta, GA, USA, 1985, 99. 30. K. Collington, Proceedings of Cellular Polymers I, Rapra Technology Ltd., Shrewsbury, UK, 1991, Paper No.22. 31. C.F. Tu, Proceedings of SPE ANTEC ’77, Montreal, Canada, 1977, 211. 32. G.L.A. Sims and C.O’Connor, Proceedings of Blowing Agent Systems: Formulations and Processes, Rapra Technology Ltd., Shrewsbury, UK, 1998, Paper No.2. 33. S. Girois and C.A. Bertelo, Proceedings of SPE Vinyl Retec ‘97: Plastic Systems for the Building Industry, Atlanta, GA, USA, 1997, 107. 34. N.L. Thomas, R.P. Eastup and J.P. Quirk, Plastics, Rubber and Composites: Processing and Applications, 1997, 26, 47. 35. J-L. Pfennig and M. Ross, Proceedings of PVC ‘90, PRI, Brighton, UK, 1990, Paper No.21. 36. K.U. Kim, T.S. Park and B.C. Kim, Journal of Polymer Engineering, 1986, 7, 1. 37. B.C. Kim, K.U. Kim and S.I. Hong, Polymer (Korea), 1986, 10, 143. 38. N.L. Thomas and R.J. Harvey, Journal of Vinyl and Additive Technology, 1999, 5, 63. 39. D.W.V. Krevelen, Properties of Polymers: their Correlation with Chemical Structure; their Numerical Estimation and Prediction from Additive Group Contributors, 3rd Edition, Elsevier, Amsterdam, 1990, Chapter 18. 40. G. Luebke, Proceedings of Blowing Agent Systems: Formulations and Processes, Rapra Technology Ltd., Shrewsbury, UK, 1998, Paper No.11. 41. D. Stover, Plastics World, 1994, 52, 7, 33.

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Rigid PVC Foam 42. M. Gale, British Plastics and Rubber, 2000, May, 4. 43. S.K. Dey, C. Jacob and M. Xanthos, Journal of Vinyl and Additive Technology, 1996, 2, 48. 44. K. Blizard, L. Chen, R. Straff, M. Deweerdt and D. Mullie, Proceedings of AMI Profiles Conference 2000, Düsseldorf, Germany, 2000, Paper No.12. 45. M.R. Holl, M. Ma, V. Kumar and R.R. Kwapisz, Cellular Polymers, 1998, 17, 271. 46. F.N. Cogswell, Pure & Applied Chemistry, 1983, 55, 178. 47. K. Kitai, P. Holsopple and K. Okano, Journal of Vinyl Technology, 1992, 14, 211. 48. J. Patterson in Plastics Additives: An A-Z Reference, Ed., G. Pritchard, Chapman and Hall, London, UK, 1998, 526. 49. P.S. Schipper and D. Tanjala, Proceedings of APE Vinyl Retec ‘97: Plastic Systems for the Building Industry, Atlanta, GA, USA, 1997, 137. 50. F. Ide and K. Okano, Pure & Applied Chemistry, 1981, 53, 489. 51. B. Haworth, L. Chua and N.L. Thomas, Plastics and Rubber and Composites Processing and Applications, 1994, 22, 159. 52. M. Cuilleret, Proceedings of Addcon World ‘98, RAPRA, London, UK, 1998, Paper No.11. 53. R.W. Decker, Journal of Vinyl and Additive Technology, 1996, 2, 121. 54. DIN 53420, Testing of Cellular Materials; Determination of Apparent Density, 1978. 55. DIN 52612, Testing of Thermal Insulating Materials. 56. DIN EN ISO 179, Plastics - Determination of Charpy Impact Strength, 1997. 57. DIN EN ISO 527-1, Plastics - Determination of Tensile Properties - Part 1: General Principles, 1996. 58. DIN EN ISO 527-2, Plastics - Determination of Tensile Properties - Part 2: Test Conditions for Moulding and Extrusion Plastics, 1996.

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Handbook of Polymer Foams 59. DIN 53505, Testing Of Rubber - Shore A and Shore D Hardness Test, 2000. 60. ISO 178, Plastics - Determination of Flexural Properties, 2001. 61. DIN EN ISO 306, Plastics; Thermoplastic Materials; Determination of Vicat Softening Temperature, 1997. 62. P.R. Hornsby, Materials in Engineering, 1982, 3, 443. 63. M.F. Ashby, Metallurgical and Materials Transactions A, 1983, 14A, 1755. 64. J.L. Throne, Plastics Design and Processing, 1976, 16, 20. 65. J. Patterson, Journal of Vinyl and Additive Technology, 1998, 4, 26. 66. K.H. Steinbruck, Proceedings of SPE RETEC ARC ‘97: Information to Grow the Plastics Recycling Industry, Chicago, IL, USA, 1997, 219. 67. R.L.J. Pots and P. Benjamin, Proceedings of Plastic Pipes IX, Edinburgh, UK, 1995, 442. 68. S. Dupont, C. Dehennau, P. Benjamin, B. Rijpkema and G. Voituron, Proceedings of Recycle ’91 Conference, Davos, Switzerland, 1991, Paper No.34. 69. N.L. Thomas and J.P. Quirk, Plastics and Rubber and Composites Processing and Applications, 1995, 25, 89. 70. N.L. Thomas, J.P. Quirk and H. Cretney, Progress in Rubber and Plastics Technology, 1997, 13, 56. 71. V. Kumar, Cellular Polymers, 1993, 12, 207. 72. J.E. Martini, F.A. Waldman and N.P. Suh, Proceedings of SPE ANTEC’ 82, San Francisco, CA, USA, 1982, 28, 674. 73. D.F. Baldwin, C.B. Park and N.P. Suh, Polymer Engineering and Science, 1996, 36, 35. 74. European Plastics News, 1998, 25, 8, 107. 75. European Plastics News, 1999, 26, 9, 27. 76.

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V. Kumar, J.E. Weller, M. Ma, R. Montecillo and R.R. Kwapisz, Cellular Polymers, 1998, 17, 351.

Rigid PVC Foam 77. M. Glaskin, Advanced Composites Engineering, 1990, 5, 5, 16. 78. G. Dohn and R. O’Meara, Reinforced Plastics, 1999, 43, 5, 22.

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7

Flexible PVC Foams Christopher J. Howick

7.1 Introduction Chapter 6 of this handbook gives a detailed description of the formulations and techniques involved in the production of rigid polyvinyl chloride (PVC) foams. As far as the end product is concerned, the only difference between a rigid PVC foam and a flexible one is the presence of a plasticising species in the latter. However, this simple chemical difference hides a major difference in the production technologies available to produce flexible foams. The majority of flexible PVC foams are produced via a plastisol route, that is, the products are spread as a liquid dispersion of a speciality PVC resin in liquid plasticiser and gelled and fused in ovens rather than produced via the rigid foam route of extrusion and injection moulding. Additionally there is a large range of plasticising species available on the open market, each with the potential of altering the foaming characteristics of the formulation. All of these will be discussed in detail in this review.

7.2 Flexible Foam Types and PVC Types

7.2.1 Flexible Foams Based on Suspension PVC In order to differentiate further, it should be stated that flexible foams can be formed from PVC resins produced by two distinct technologies. Suspension PVC resins (S-PVC), as used in rigid foams, can be used to form both rigid and flexible articles. For flexible articles, a plasticiser, usually a liquid (see next Section), is added in the dry blend stage of production and this remains in the final product to give flexibility to the resin. The processing technology of the dry blend is the same as those for rigid systems although due account needs to be given to the lower melt viscosity and reduced fusion temperatures of the plasticised formulation. In principle any rigid foam application can be made flexible by this route although applications for flexible foam via this route are somewhat rare. The products themselves tend to have a low melt strength.

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7.2.2 Flexible Foams Based on Dispersion or Paste Resins A very high proportion of flexible PVC foams are based on dispersion or paste resins. These are materials produced from a wide variety of speciality PVC resins - emulsion, seeded emulsion, microsuspension, mini-emulsion - which have the capability of forming a liquid dispersion or plastisol when mixed with a liquid plasticiser. These resins, compared to their S-PVC counterparts, are very fine particle size powders produced by the spray drying and milling of a PVC latex. Plastisols formed from these resins can be spread, rotationally cast, sprayed or have other substrates dipped into them. The wet plastisol is then gelled by various routes but usually this is done thermally with a conventional oven. In simple terms the incorporation of a blowing agent, usually azodicarbonamide (ADC), during the plastisol mixing stage, will produce a foamed article in the oven. The higher the level of blowing agent used the greater the level of expansion in the final product and consequently the lower the density of the final product. This is the production of chemically foamed flexible PVC but the production of mechanically foamed flexible PVC is also possible. This is formed by the deliberate incorporation of air into the plastisol in the mixing stage and if this ‘wet foam’ can be maintained during the fusion stage a foamed product will result. The production of foam by this route is particularly enabled by dispersion resins since in general they contain residual surfactant which can act to stabilise the wet cells, although the deliberate addition of further surfactant is also commonplace. This process is described in more detail in the application sections (Sections 7.3.1 and 7.3.4).

7.2.3 Chemically Blown Foams from PVC Plastisols: Fundamentals Details of applications for plastisol foams are given in Section 7.3 and references [1-3] of this review but all applications of chemically foamed plastisols are governed by the same general principles. The chemical blowing agent is introduced into the formulation during the plastisol mixing stage along with other ingredients. A typical foamed plastisol formulation will contain the following: • • • • • • • •

PVC Dispersion resin Mineral filler (chalk) Pigment Liquid plasticiser Blowing agent Stabiliser/kicker (activator) Viscosity depressant Speciality additives

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Flexible PVC Foams Each of these in turn has a pronounced effect on foam formation and are discussed individually below, but first a description of the normal gelation and fusion processes involved in the formation of a plastisol-based PVC foam is given.

7.2.3.1 Plastisol Foam Formation The formation, gelation and foaming of a plastisol can be divided into a number of key steps: •

Plastisol Formation

The PVC resin and other additives (including chemical blowing agent) are mixed in a planetary or impellor type mixer to form an even dispersion of all the solid ingredients in the liquid phase. For low viscosity pastes it may be necessary to instigate a two fold mix cycle with a reduced amount of liquids in the first cycle to ensure a higher viscosity mix to give adequate dispersion of solid particles in the mix. This is particularly important when the blowing agent in use is in solid form since uneven dispersion of blowing agent will result in uneven expansion in the foam. Chemically foamable plastisols are then usually evacuated to remove excess air. The plastisol may be stored or used immediately. •

Coating

The plastisol is coated onto a substrate or poured into a mould. By far the most common means of application is onto a substrate (for floorings, wallcoverings, coated fabrics, synthetic leathers). Application of the plastisol to the substrate is made by using reverse roll, knife coating or screen coating, each of which place a different viscosity and rheology requirement on the plastisol. A good review of these techniques in the wallcovering sector is given by Niven [4] and the general rheology of PVC plastisols by Sarvetnick [5]. •

Semi-gelation

The coated substrate may then be semi-gelled if subsequent coats and print designs are to be applied. This involves heating of the plastisol to above the glass transition temperature of the PVC polymer (70-85 °C) so that the polymer chains become fully mobile and the plasticiser and other liquid additives can be absorbed into the polymer. This results in a rapid rise in viscosity as the plastisol solidifies and for a typical midmolecular weight resin this state continues until the temperature reaches approximately 140 °C. This is a typical semi-gel temperature although the range varies from 125 °C to 160 °C depending on both polymer and formulation. The state of the semi-gel is a solid

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Handbook of Polymer Foams but as complete fusion of the polymer and all the additives has not yet occurred the material has little strength and flexibility. However if the semi-gel has been produced by passing the plastisol around a heated drum, as is frequently the case, the semi-gel has a very smooth surface which is ideal for printing of designs or the laying down of further plastisol coatings. One key point for semi-gelled plastisol foams is that the semi-gel temperature must be below both the true decomposition temperature and the catalysed decomposition temperature of the blowing agent to prevent foaming and surface texturing of the semi-gel. •

Gelation, Fusion and Expansion

After semi-gel printing and storage the material is then fused by passing through another heating stage. This stage is normally performed using conventional thermal ovens. During fusion the polymer enters the melt and full mixing of formulation ingredients occurs at a molecular level. The result of the melting of the polymer is for a reduction in viscosity to take place. The overall viscosity versus temperature profile for a typical plastisol in shown in Figure 7.1. On cooling from the fused state the product re-establishes the polymer network but with plasticiser molecules intimately mixed. These molecules prevent the establishment of all of the chain - chain interactions that characterise rigid PVC so the flexibility of the final product is greatly enhanced (for detailed descriptions of the plasticisation mechanism see [6-11]).

Figure 7.1 Effect of plasticiser level of plastisol gelation and fusion

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Flexible PVC foam Flexible PVC Foams For the purpose of flexible PVC foams, the key point about the gelation and fusion process is that the temperature of the blowing agent decomposition will be reached and exceeded during this stage. The resulting generation of gas will give rise to the foaming of the melt and this structure will be retained in the final product if cell walls have sufficient strength to survive the thermal treatment after they have formed. The amount of foam expansion depends on a number of factors but in simple terms is governed by the volume of gas generated and the viscosity of the polymer melt at the point of blowing agent decomposition, higher viscosity melts giving a greater level of resistance to the expanding gas. There are many good detailed descriptions of the foaming of PVC plastisols given in the literature [1-3] and the reader is encouraged to read these to gain an indepth understanding.

7.2.3.2 Blowing Agents and Foam Formation A chemical blowing agent is a substance that can be added to a material such that the substance decomposes at a given temperature to release a volume of gas that causes the material to expand. As with rigid foams by far the most common chemical blowing agent is ADC which has a decomposition temperature in the range 200-230 °C. This temperature can be reduced by the incorporation of catalysts or ‘kickers.’ These are typically metal salts or complexes and have chemical features so much in common with the range of metal thermal stabilisers for PVC that the two properties are frequently combined in a ‘stabiliser - kicker’ system. These can be used either separately from the blowing agent or they can be compounded with the blowing agent by the blowing agent manufacturer. Thus in theory it is possible to tailor a blowing agent-kicker combination for an individual formulation and set of processing conditions to give the degree of gas yield and expansion required. In addition to the temperature of blowing agent decomposition the rate of gas generation is also critical and depending on the processing conditions (length of oven, rate of air changes, etc.), a choice of kicker will need to be made. Four basic types are: 1. Low temperature action with rapid gas generation 2. Low temperature action with slow gas generation 3. High temperature action with rapid gas generation 4. High temperature action with slow gas generation and there are also intermediate types available from suppliers. The effect of these various kickers is shown in Figure 7.2. For example a high speed wallcovering formulation based

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Figure 7.2 Effect of different kickers on foam expansion

on a low molecular weight resin would require a low temperature, rapid gas generation type since the low molecular weight of the resin would establish the correct melt viscosity conditions rapidly. In a product which has additional requirements of mechanical strength a higher molecular weight of PVC resin will be specified with the proviso to delay the decomposition of the blowing agent until the plastisol melt viscosity has reduced sufficiently to give the expansion level required. This may result in the need for a high temperature, more controlled gas generation kicker/catalyst type. However raising the molecular weight of the PVC resin can be of limited effect in an attempt to improve the mechanical strength of the foam: greater benefit in mechanical strength can often be obtained by improvements in the structure and uniformity of the foam produced and in many cases this may mean the use of low molecular weight PVC homopolymers.

7.2.3.3 Cell Types Flexible PVC foams are generally described by their cell nature, i.e., closed or open cell. Closed cells tend to give good resistance to compression but if compression occurs they will recover slowly. Open cells, whilst offering very low resistance to compression, will recover quickly from any compressive force. These factors are important where these

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Flexible PVC Foams properties form part of a specification. Generally an open cell structure will result if a large amount of the foam structure has formed before maximum gelation of the plastisol has occurred. When further heat is applied and melt viscosity falls, the pressure within an individual cell increases so that the cell walls break to form an open cell structure. Thus for open cell structure a fast gelling system is desired and this can be made through formulation development and resin choice. Although some statements with regard to preferred resin choice for open and closed cell have been made [1] exceptions to these statements can be found. In addition to the type of cell, i.e., whether open or closed type, the quality of the cell will also need consideration. Cells can range from exceedingly fine to very coarse and this is controlled by a number of factors. Of key importance are the gelation rate, the gas evolution rate of the blowing agents involved and also the surfactant present from the PVC resin manufacturing process. The PVC particles will contain a layer of surfactant on their surface and when the blowing agent decomposes these layers stretch so the surface tension of this surfactant plays an important role in determining the quality of the cell (as defined by structure (open or closed), size and uniformity), as does the solubility of this surfactant in the plasticiser and the ease at which the plastisol can release entrapped air (for chemical foaming formulations) or retain air (for mechanical foam formulations). PVC resin manufacturers will generally develop resin systems for chemical foam formulations of given families of surfactants known to impart good cell structural quality.

7.2.4 PVC Resins used in Plastisol Foam Formation The choice of PVC resin in the chemically foamed formulation has long been a subject which arouses great amounts of discussion and debate. Since these resins are spray dried they tend to have a unique particle size distribution associated with the drying process, which is difficult to match on a different spray drier. Consequently, different resins have different particle size distributions and hence different gelation properties which in turn affect the foam properties. Although end users may deem one resin as an acceptable alternative to another resin, it is rare to find two resins which are indistinguishable. Resins available are made by a variety of routes.

7.2.4.1 Microsuspension Resin Made in a method similar to the suspension resin (in which monomer droplets are suspended in water and then polymerised using a monomer soluble initiator) with the exception that the vinyl chloride:water mixture is mechanically homogenised to produce very fine droplets of monomer in water. These droplets are then stabilised using a surfactant and the system polymerised. This results in a broad particle size PVC latex which is then spray dried and milled.

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7.2.4.2 Emulsion Resins In this case the polymerising medium contains very small droplets of monomer in water which are formed by the use of surfactants. The polymerisation is carried out using water soluble initiators and the resulting PVC latex contains very small PVC particles with a very narrow particle size distribution. This latex can then be spray dried and milled. A number of variants of the process are also available such as seeded emulsion, continuous emulsion and mini-emulsion. The last of these shows similarities to microsuspension polymers in that a broad range of monomer droplet sizes are formed through the use of surfactants. Emulsion and seeded emulsion polymers may be differentiated from mini-emulsion polymers in that for the latter a homogenised mix of vinyl chloride monomer and water is produced prior to polymerisation through the use of surfactants. This combined surfactant system (where surfactants act to both homogenise the monomer:water mixture and to take part in polymerisation) generally leads to polymers possessing relatively high residual surfactant levels and these can play a part in the foaming process since they can lead to a differing surface tension of the expanding cell walls during the formation of the foam. In general terms such polymers exhibit faster gelation properties and a tendency to open cell formation, a property that can be enhanced by careful selection of blowing agents and kickers. The drying and milling phases of the processes - common to all of the polymerisation technologies listed above - play a critical part in the foaming performance of the grade of polymer. The spray drying process forms agglomerates of the primary particles present in the PVC latex. These can range from a few microns in size up to about 50 μm. These agglomerates can be broken down by milling although it is rare for large proportions of them to be broken down entirely. As a result, the final polymer as supplied to the foam processor contains a range of particles from sub-micron primaries to persistent large agglomerates up to 50 μm. The proportion of agglomerates to primaries is set by the precise drying conditions and the severity of the milling used. Essentially the smaller particles melt more quickly on the application of heat which then results in the plastisol entering the true melt phase more rapidly.

7.2.5 Mineral Fillers Fillers such as chalk are used in a formulation for cost reasons since they are normally available at significantly lower costs than the other primary formulation ingredients. The level used is a balance between the cost advantages and the potentially detrimental effects on foaming and viscosity of the plastisol. High filler levels will lead to an increased melt viscosity which will in turn provide more resistance to the evolved gas from the blowing agent decomposition. In turn this will lead to reduced foam expansion. High

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Flexible PVC Foams filler levels will also result in higher densities of the foam (filler density is significantly higher than other formulation ingredients) and result in a deterioration in mechanical properties. At high levels, filler will also have an effect on the cell structure.

7.2.6 Pigments These have a similar effect to fillers but, owing to their significantly higher price and the fact that they have the potential to cause increased plastisol viscosity, their concentration in the final formulation is significantly lower than that of a filler and in normal cases their effect on foaming is negligible.

7.2.7 Liquid Plasticiser This has a pronounced effect on the foaming process, both in terms of type and levels used. Since foaming properties are dependent on the melt viscosity of the plastisol, plasticisers play an important part in the foaming process since they can, by nature of their polarity and concentration, affect the melt viscosity obtained during the fusion process. It needs to be stressed that a conventional viscosity versus temperature plot as recorded using dynamic temperature viscometry, records the change in viscosity with temperature over a period of up to 30 minutes whereas conventional plastisol fusion ovens subject the plastisol to a high temperature, e.g., 200 °C, for a short time period (1-2 minutes). Thus, the time taken for a plastisol to reach a given melt viscosity will be controlled by the fusion characteristics of the formulation. In general, faster fusing formulations will give faster expansion owing to their ability to reach lower melt viscosities during the plastisol fusion stage. In terms of plasticiser types, the effects are summarised next: •

‘Active’ plasticisers: these produce fast fusing systems and are generally based on polar, relatively low molecular weight plasticiser esters such as butylbenzyl phthalate and benzoates. Whilst these produce fast fusion and relatively fast expansion it should be noted that the higher polarity can cause relatively rapid rates of plastisol viscosity increase with time and may lead to undesirable migration and exudation properties in the final product.

•

Dialkyl phthalate esters: these include the industry standards di-2-ethylhexyl phthalate, di-isononyl phthalate and di-isodecyl phthalate (DIDP). Such esters also includes diisoheptyl phthalate.

The effect of these plasticiser types on the foam properties are given in Table 7.1.

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Table 7.1 Effect of plasticiser type on fusion and foaming characteristics Phthalate ester

No of carbon atoms in alkyl chain

Fusion and foam characteristics

4 and 6

Very fast

Dipropylene glycoldibenzoate

3

Very fast

Di-isoheptyl phthalate

7

Fast

Di-2-ethylhexyl phthalate

8

Medium

Di-isononyl phthalate

9

Medium

Di-isodecyl phthalate

10

Slow

Linear 9,11 phthalate

9 and 11

Slow

Di-undecyl phthalate

11

Slow

Di-isotridecyl phthalate

13

Very slow

Butylbenzyl phthalate

The plots shown in Figures 7.1 and 7.3 record the changes in viscosity of the plastisol with temperature and this can be used to find the optimum range of melt viscosity for a given blowing agent system. The key parameter is the precise value for the viscosity of the plastisol melt at the temperature of decomposition of the blowing agent. Figure 7.1 shows the effect of increasing the level of plasticiser on the gelation characteristics with progressive additions resulting in progressive reductions in melt viscosity which in turn will produce greater foam expansion when the blowing agent decomposes. Similar effects can be obtained from increasing mineral fillers (increasing melt viscosity) and decreasing the molecular weight of the resin (K Value) which leads to significant reductions in melt viscosity and therefore greater foam expansion during blowing agent decomposition. Figure 7.3 shows the effect of different plasticiser type on the gelation characteristics with the very active butyl benzyl phthalate giving rapid gelation through to the relatively slow progress of the C10 phthalate ester DIDP. Also shown here is the plot of Tan delta with temperature. This is the ratio of the loss (or viscous) modulus to the storage (or elastic) modulus of the plastisol. Since a PVC plastisol is neither purely viscous (dissipating all energy as heat during flow and not recovering to any degree from the deformation), nor purely elastic (storing all energy input and recovering completely from the applied deformation) this value gives a measure of the change in state of the plastisol as the temperature is raised. In turn this gives a measure of the elasticity of the plastisol at a given temperature as the plastisol is heated and this can give an insight into its ability to

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Figure 7.3 Effect of plasticiser type on plastisol gelation and fusion

be used satisfactorily in certain processes in which the material may be subject to deformation at various temperatures. Figure 7.3 shows the expected increase in Tan delta (increasing viscous behaviour) as the plastisol enters the melt.

7.2.8 Blowing Agent Type and Level Naturally this is a critical feature of foam formation. Whilst the level of foam increases proportionately with the level of blowing agent, higher levels of blowing agent may lead to a disruption in the texture of the foam surface. Birch [12] showed the relationship between blowing agent particle size and speed of expansion: as expected a finer particle size of the blowing agent results in a more rapid decomposition that a corresponding large particle size blowing agent. ADC continues to be the standard for the flexible PVC industry since it is relatively easily activated with foam catalysts (or ‘kickers, see Section 7.2.3.2) so that the decomposition occurs in the melt range for the majority of PVC resins. Where lower plastisol gelation temperatures are used other lower temperature blowing agents such as 4,4´-oxy bis(benzenesulfohydrazide) can be used. Additionally, inorganic hydrogen carbonates can also be used. These are seldom used alone but may be used to augment ADC and in some cases can produce desirable surface effects in fashion goods. There has recently been a move towards very matt finishes for foam surfaces as a desired fashion effect and producers have faced a technical challenge in ensuring that technology and additives available to provide surface disruption on a microscopic level have not led to a deterioration in foam quality.

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7.3 Products Utilising Foamed Plastisols A number of industries utilise flexible PVC foam technology. The principal ones are: 1. Floorings and carpet backings 2. Wallcoverings 3. Synthetic Leather 4. General Foams

7.3.1 Floorings and Carpet Backings Whilst these can be made through a calendered route the foamed products are generally made through a plastisol route. The spread (plastisol) flooring market can be divided into two distinct sectors - domestic and contract. The former places a major emphasis on design and new designs both instigate and follow fashion trends within the sector. There are regular new product launches and the foam can play an important part in the achievement of these design requirements. A typical cushion vinyl flooring consists of four layers (see Figure 7.4). At the top is a wear layer of clear PVC which provides the necessary wear and mechanical resistance. Beneath this there is generally a printed foam layer which utilises chemical inhibition. Both of these layers are spread onto a fibreglass layer impregnated with a solid PVC plastisol. The whole assembly can then be turned and have a backing layer applied and the whole flooring can then be fully fused during which time expansion of the blowing agent occurs.

Figure 7.4 Typical cushion vinyl flooring: 1 = Impregnated fibreglass; 2 = printable foam layer; 3 = clear wear layer and 4 = foamed backing layer (chemical or mechanical)

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Flexible PVC Foams The aim of the process of chemical inhibition is to nullify the effect of the blowing agent. The printable foam coating is spread onto the solidified coated fibreglass and this new layer is then gelled at a temperature below the decomposition temperature of the blowing agent. This stage is performed frequently using a heated metal drum. This solid product is then printed with inks, some or all of which can contain a chemical inhibitor, which either interacts with the blowing agent to prevent its decomposition, (e.g., thiourea), or interacts with the kicker to prevent it from ‘kicking’ the blowing agent (trimellitic anhydride, benztriazole). Whichever route is used the effect is the same - selective prevention of foaming in the layer to give a contour effect, (i.e., areas of foam and areas of no foaming), throughout the flooring. Since these inhibitors may be dispersed or dissolved in selected inks only, this leads to certain colours in the design possessing differential relief to other colours when the remaining PVC layers have been applied and the final product is expanded by fusion - a potentially striking visual effect. An alternative method can involve the inclusion of kickers in the ink so that foaming is generated only in printed areas - again the overall effect is the same. The inks are then dried and other layers applied. The original technology was patented by the Congoleum Corporation [13] although the primary patents have expired and the technique is now used throughout the cushion vinyl flooring industry. Traditional inhibitors were based on trimellitic anhydride although concerns with regard to the toxicity of this material have encouraged the use of benztriazole. More recently technology has moved towards water-based printing systems and derivatised benztriazole and thiourea systems have been studied. Today a number of proprietary inhibition systems are sold. It may be noted that the mechanism of inhibition requires migration of the inhibiting species into the printable vinyl layer. The rate of this migration will depend on both the migration rate of the ink solvent and the thickness of the foam layer. It is possible to dry these inks too rapidly before full penetration has occurred (especially in the case of the generally less polar, water-based systems) and also there is a danger of excessive migration if the unfoamed, semi-finished product is stored for prolonged periods. This is due to the migration of the ink continuing under pressure in the rolled flooring through other layers and into the foamed areas that are not intended to be inhibited. This phenomenon is generally referred to as ‘ghosting’ [4]. The backing layer is frequently foamed, either by a chemical or mechanical means. In this layer foam structure is important since it is this layer which is a major contributor to the ‘cushion’ effect. Contract vinyl flooring possesses many of the features of cushion vinyl flooring. Whilst design and fashion are important, a major consideration is meeting the key technical standards specified by authorities or architects for installation in hotels, schools, hospitals,

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Handbook of Polymer Foams etc. Key areas in which PVC foam has a major contribution are the acoustic properties and the compression and indentation resistance and recovery. The products used in this area have a variety of structures, e.g., printed inhibition type foams, flat printed layers, thick or thin wear layers, compact or highly foamed backings selected to obtain the overall properties required to meet these tests. The foam contributes thickness and a cellular structure, with thick, closed cell foams preferred for sound absorption. For good compression properties, closed cell foams offer better compression resistance although open cell foams perform better on compression recovery. The exact requirements are generally met by a suitable combination of resin type, expansion ratio, fusion conditions and foam thickness. Standards of relevance are EN 424 [14], EN 425 [15] and EN 433 [16]. Acoustic properties of building materials form one of the six essential requirements of the European Construction Products Directive (89/106/EEC) [17]. The production of foamed PVC backings for carpets also takes place although the volumes involved are much lower than that for cushion vinyl floorings. Application technologies are relatively straightforward knife coating technologies and are based on free foaming formulations, (i.e., no inhibition requirement). A range of blowing agents is used. ADC is the most common although lower temperature systems can also be used when either carpet fibres or printing inks used in the carpets are particularly thermally sensitive. Some products in this sector are sold into contract applications and here acoustic and compression recovery is also important although the carpet itself has a major influence on these properties.

7.3.2 Wallcoverings Foamed wallcoverings show many of the foaming technologies described for floorings although the foaming in wallcoverings is almost exclusively through a chemical rather than mechanical means. A variety of foamed wallcoverings are available: 1. Inhibited foamed wallcoverings 2. Free blow foams with flat surface 3. Free blow foams with a textured surface Inhibited foamed wallcoverings are made using the same methodology as described for the inhibition layer of cushion vinyl flooring. In wallcoverings this produces a relief effect and gives the ability for the wallcovering producer to mimic a tile design (hence this particular product being named ‘tiling on a roll’). The technology was again based on the Congoleum patent [13]. This product may also contain a clear PVC coating on top.

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Flexible PVC Foams Relief designs in wallcoverings can also be made by printing foamable plastisols onto paper in a specific design through screen printing. The versatility of PVC resins available on the market enables all types of rheology to be obtained and this includes the highly pseudoplastic rheology, required for high speed screen printing of intricate designs. With good shear recovery plastisol can be laid down onto paper without flowing out of design so that the plastisol is fused with blowing agent decomposition in specific areas to create the desired design effect. With numerous screen printing stations available, each printing a plastisol with a different formulation (often containing a different level of blowing agent), complex designs are possible with different areas having different levels of expansion. Many of these designs have areas of high expansion but with characteristic flat surfaces - an effect requiring complicated PVC formulating involving resin, plasticiser, blowing agent and kicker development. The surface texture can be altered by precise changes in the melt viscosity profile in order to find the optimum melt viscosity at the temperature at which the blowing agent decomposes. Similar designs can also be produced with a textured surface. In this case the surface of the foam is deliberately disrupted through a combination of ‘pre-blow’, caused by the incorporation of low temperature blowing agents, and by the incorporation of a volatile species - frequently iso-propanol - to allow for boiling off during the foam gelation stage. This textured surface is a traditional design feature for certain markets.

7.3.3 Synthetic Leather This is a large market for plastisol-based PVC resins and the foaming of plastisols is an integral part of the technology. The product itself is made up of a number of layers (see Figure 7.5). A plastisol is applied to a backing substrate such as a silicone release paper and gelled. The foam layer is then applied and gelled below the decomposition temperature of the

Figure 7.5 Schematic of PVC leathercloth; 1 = fabric backing; 2 = foam layer; 3 = solid top coat; 4 = release paper or other substrate

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Handbook of Polymer Foams blowing agent. A lamination plastisol is then applied and finally a fabric (either natural or synthetic) is applied and ‘squeezed’ into the lamination plastisol. The whole assembly is then fused in an oven and the blowing agent allowed to decompose. In some cases the lamination stage may be omitted and the adhesion of the fabric simply made into the foam coat. The general aim of the product is to have a relatively high expansion ratio to simulate the lightweight leather ‘feel’ - indeed, in many of the fashion leather sectors this ‘feel’ or ‘touch’ is the main selling point and is difficult to quantify in terms of mechanical testing. The lightness is also enhanced by relatively high levels of plasticiser and here resin choice is important since a resin which is capable of giving a workable paste with high levels of plasticiser is required. In technically demanding sectors such as automotive leather, additional requirements exist. Many systems omit the fabric stage and these products are known as unsupported expanded vinyl (UEV) and in this case the PVC must possess additional strength since it cannot rely on the fabric for strength in the many vacuum forming processes that exist in the automotive industry. This places the additional challenge to the PVC formulator since the additional mechanical strength is generally obtained through the use of higher molecular weight resins which traditionally possess poorer foaming characteristics. Hence a formulation requiring higher foaming temperatures and later blowing agent decomposition (see above) may be appropriate. Additionally this product must possess low fogging properties and have excellent long term thermal stability.

7.3.4 General Foams In addition to those products described previously, foams are also produced and sold as foams. These products are generally highly expanded and subsequently low density chemical foams or low density mechanical foams produced by speciality processes. These products sell into markets such as the automotive and indoor application markets for sealing foams and products such as draft excluders. They are technically demanding since the general requirement is to obtain very thick foams (in comparison to the products described previously) but still retain a fine cell structure which is free from foam collapse and possesses a flat foam surface. Such foams are also made through simple plastisol coating technology and differ only in the significantly higher levels of blowing agents used. Foams are generally sold according to density and indentation resistance and recovery specifications and in some cases the proportion of open to closed cells. Some speciality foams are produced through mechanical means involving the pressurisation of a PVC plastisol with a liquid blowing agent which will evaporate to produce a foamed plastisol which can then be gelled. The foam is normally produced in very thick slabs which can then be cut into thinner sections as required. Again these find

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Flexible PVC Foams use in automotive applications but also in stationery goods and sports matting and medical applications such as surgical collars.

References 1.

R. Brathum and P. Zingsheim in Polymeric Foams, Eds., D. Klempner and K. Frisch, Hanser Publishers, Munich, Germany, 1991, Chapter 10.

2.

D.A. Boscott and S. Coulson, Proceedings of PVC ‘93, Brighton, UK, 1993, Paper No.36.

3.

P. Bergounhon and B. Ernst, Proceedings of PVC ‘99, Brighton, UK, 1999, p.258.

4.

W.G. Niven in Plastics: Surface and Finish, 2nd Edition, Ed., W.G. Simpson, Royal Society of Chemistry, Cambridge, UK, 1993, Chapter 15, p.281-305.

5.

Plastisols and Organosols, Ed., H.A. Sarvetnick, Van Nostrand Reinhold, New York, NY, USA, 1972.

6.

J.K. Sears and J.R. Darby, The Technology of Plasticizers, Wiley Interscience, New York, NY, USA, 1982.

7.

A. Wilson, Plasticisers: Principles and Practice, Institute of Materials, London, UK, 1995.

8.

D.F. Cadaogan and C.J. Howick in Ullmann’s Encyclopedia of Industrial Chemistry, 5th Edition, VCH-Wiley Publishers, New York, NY, USA, 1992, Volume A20, p.439.

9.

D.F. Cadogan and C.J. Howick in Kirk-Othmer Encyclopedia of Chemical Technology, 4th Edition, John Wiley and Sons, New York, USA, 1996, Volume 17, p.258.

10. C.J. Howick, Proceedings of PVC ‘93, Brighton, UK, 1993, Paper No.38. 11. N.J. Clayden and C.J. Howick, Polymer, 1993, 34, 12, 2508. 12. S.J. Birch, Proceedings of PVC ‘93, Brighton, UK, 1993, Paper No.35. 13. J.C. Harkins, Jr., R.R. Nairn, H. Tarlow and F.E. Ehrenfeld, inventors; Congoleum Nairn Inc., assignee; US 3293094, 1966.

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Handbook of Polymer Foams 14. EN 424, Resilient Floor Coverings – Determination of the Effect of the Simulated Movement of a Furniture Leg, 2001. 15. EN 425, Resilient Floor Coverings – Determination of the Effect of a Caster Chair, 2002. 16. EN 433, Resilient Floor Coverings – Determination of Residual Indentation After Static Loading, 1994. 17. 89/106/EEC, Council Directive of 21st December 1988 on the Approximation of Laws, Regulations and Administrative Provisions of the Member States Relating to Construction Products, 1988.

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Polyolefin Foams

8

Polyolefin Foams David Eaves

8.1 Introduction Although polyolefin foams are relatively recent additions to the range of polymeric foam materials, having been first marketed in the early sixties, they have found a use in almost every industry. Areas of application include packaging, sports and leisure, toys, insulation, automotive, military, aircraft, buoyancy, cushioning and others. This wide range results from the scope to vary properties from hard and tough through to soft and resilient. Hard (though not brittle) foams are obtained using polypropylene or high density polyethylene as the basic polymer, whilst softer materials are obtained using ethylene or propylene co-polymers such as ethylene vinyl acetate (EVA). This ability to vary foam properties by changes in the polymer is similar to that seen in polyurethane foams, although the technologies are very different since almost all polyurethane foams result from liquid technology with in situ polymerisation and blowing whilst polyolefin foams are all produced starting with the basic thermoplastic polymer. No single foaming method dominates polyolefin foam manufacture and both continuous and batch processes are operated. The manufacturing process is a factor determining both the form of the foam (sheet, block, bead) and foam properties since the process determines the foam structure, degree of crosslinking (if any) and level of residual byproducts, e.g., from the blowing agent. Polyolefin foams are normally closed cell, though open cell products can be made by a post manufacture processing operation. The foams may be crosslinked or non-crosslinked, different processes being used for each type. Crosslinked foams retain their basic foam structure at temperatures above the polymer melting point and hence lend themselves to heat moulding methods for the manufacture of shaped products from foam sheet. Most polyolefin foam products involve further operations on the foam following manufacture. Whilst there has been for some time a wide choice of materials for polyolefin foam manufacture encompassing most of the homo and copolymers of ethylene and propylene, the range has recently been increased further by the introduction of polyolefins made

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Handbook of Polymer Foams using metallocene catalysts. These catalysts enable a high degree of control of polymer structure and polymers are available having enhanced properties including higher tensile strength and elongation and greater flexibility. Some manufacturers have introduced foams based on metallocene catalysed polymers and claim significant property advantages for such foams. It is reported however, that metallocene polymers are more difficult to process and hence increase the costs of foam manufacture. The blowing agents used for polyolefin foams include chemicals such as azodicarbonamide (ADC), liquids (such as chloroflurocarbons (CFC) or more recently hydrochloroflurocarbons (HCFC) and hydrocarbons) and gases (such as CO2 or N2). Since the foams are closed cell, the blowing agent remains in the foam for significant, sometimes quite extended, periods and can affect foam properties and post manufacturing forming operations.

8.2 Manufacturing Processes and Materials 8.2.1 Extruded Non-Crosslinked Foam

8.2.1.1 Process The manufacturing concept is comparatively simple, a physical blowing agent, originally CFC-11, is injected at the end of the melt homogenisation section of a single stage extruder. At this point all additives, which may include nucleating agents and pigments (often added as masterbatches), have been incorporated. The blowing agent is dispersed in the melt, reducing the melt viscosity and allowing efficient cooling and temperature control so that the melt temperature is reduced to a point close to the polymer melting point. The extruder barrel and die design are such as to withstand the high pressures generated (typically 15-20 MPa) where the liquid blowing agent is present. On exit from the die, the polymer immediately expands by virtue of the pressure from the contained blowing agent. Nucleation takes place in the die as the pressure decreases towards the die exit and may be enhanced by the presence of nucleating agents such as talc. Adiabatic cooling effects help to stabilise the polymer by reduction of extrudate temperature below the polymer melting point. A preferred process is a tandem extrusion system. This, whilst more capital intensive, allows separation of the initial melt homogenisation step from the subsequent mixing of blowing agent for which a higher screw speed may be necessary. A co-rotating twin

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Polyolefin Foams screw extruder is sometimes used for the primary mixing to give superior dispersion of additives. The tandem arrangement is particularly advantageous at high extrusion rates (above 200 kg/h) and allows a wider range of formulations to be processed. The high pressure generated in the down stream extruder must be contained by a suitable seal between extruders and manufacturers have their own patented solutions to this problem. After manufacture, the blowing agent within the foam can cause dimensional instability due to the different rates of diffusion of air into the foam and blowing agent out. Manufacturers therefore institute a maturing period to allow the foam to stabilise before dispatch to customers. This can take several weeks, depending on foam thickness and the temperature used to accelerate maturing. Vapour released is collected and recovered or exhausted. The use of CFC-11 has been discontinued in developed countries in line with the Montreal Protocol, and alternatives evaluated have included HCFC, HFC, various hydrocarbons such as pentane and isobutane, and gases such as CO2 and N2. Although HCFC have been adopted for the manufacture of some non-polyolefin foams, they are interim substances due for phase out themselves. HFC are acceptable but expensive, and the gases are difficult to use requiring very high containment pressures to achieve useful expansion levels. Hence, hydrocarbons have been generally adopted for the manufacture of non-crosslinked extruded polyolefin foam. Although technically acceptable in that the expansion process can, with some adjustment to material and process parameters, be made to operate satisfactorily, hydrocarbons are inherently flammable and (in mixtures with air) explosive. This gives rise to safety considerations in both manufacture and use, for instance if there is any residual vapour left in the foam after manufacture it will slowly diffuse out and, in confined storage, build up to a dangerous level. For this reason it is necessary to control the maturing stage to the extent of ensuring no significant traces of hydrocarbon blowing agent are left in the foam. Processes using an inert blowing agent do not, of course, have the flammability problems associated with hydrocarbons. Nitrogen has been in use for many years to produce crosslinked foams by the autoclave process (see later) but an extrusion process has not been developed owing to the high pressures necessary to achieve significant incorporation of gas in the polymer. Carbon dioxide however has considerably greater solubility and maintains the advantage of low cost and zero ozone depletion potential (ODP). Extrusion processes using CO2 are available, the main problem being sealing in the extruder to retain the necessary pressure. Foams however tend to have a poor cell structure with large cell dimensions, and the high diffusion rate of CO2 out of the foam compared with air into the foam results in the dimensional stability problem mentioned earlier. Extrusion processes using CO2 tend to be sensitive to operating parameters.

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Handbook of Polymer Foams Technology for production of non-CFC blown polyolefin foams is available from extruder manufacturers such as Reifenhauser GmbH (RElcell lines) and Berstorff GmbH (Schaumex and Schaumtandex lines). A typical Schaumtandex line comprises [1]: •

Silos for raw materials (polymer and reclaim).

•

Pre-dryer.

•

Mixing and metering unit for polymers and any additives.

•

Blowing agent storage vessel and metering unit.

•

Tandem extruder system with gear pump and extrusion die, e.g., for board sheet. Blowing agent is metered in towards the end of the first extruder with a patented ‘active melt seal’ to prevent back up of pressure from the blowing agent.

•

Thickness calibrator following the die.

•

Take off roller train.

•

Cooling section.

•

Take off unit.

•

Longitudinal cutter.

•

Cross cutter.

•

Conveyor belt to stacking unit.

Depending on precise design and equipment, this type of line is suitable for both polyolefins and other polymers such as polystyrene. Blowing agents can include CO2 and hydrocarbons. MuCell technology, which aims to produce foams with very small cells having dimensions comparable to or smaller than the critical flow size in polymers, also claims to produce CO2 blown polyolefin foams by an extrusion process. Foam densities however are relatively high. This recent technology is available for license from Trexel and is reviewed in Chapter 10 of this Handbook.

8.2.1.2 Materials The polymer most used is low density polyethylene (LDPE), that is, polyethylene produced by high pressure reactor technology and having a polymer density about 920 g/l. This

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Polyolefin Foams material has good processing characteristics and a suitable polymer melting point. Polymers such as linear low density polyethylene (LLDPE) and high density polyethylene (HDPE) have higher melting points with a narrower melting range, and more critical processing characteristics including lower melt strength, making these materials less suitable for the process. Polypropylene, like HDPE, also normally has a sharp melting transition and low melt strength, but some variants introduced by Montell (Higran) and Borealis (Daploy HMC 130D) introduce long chain branching into the normally linear chain structure. These products exhibit high melt strength and strain hardening which enables the production of polypropylene foams. The cell walls stabilise without rupture within the short time required to allow expansion to low densities [2]. These materials can also be used for the manufacture of expanded polypropylene beads (EPP) by extrusion (see later). An interesting material’s variant is the use of thermoplastic elastomers (TPE). Mack and Meyke (Berstorff) [3] have described a process, introduced in 1995, which uses a single extruder having an L/D of 30 with the injection point for blowing agent mid-barrel. At this stage the melt temperature is 220 ºC, reducing to 195 ºC at the die exit by virtue of the provision of barrel cooling. The profile is quenched with spray nozzles over a belt conveyor. Water is used as the blowing agent, and the polymer used is Santoprene. No nucleating additives are necessary - it is surmised that the dispersed rubber phase of the TPE is sufficient to cause bubble nucleation and a fine cell structure is produced. Foam densities are fairly high - about 300 kg/m3. The product is seen as an alternative to vulcanised ethylene-propylene diene terpolymer (EPDM) foam profiles with the advantages of: •

no curing,

•

no harmful emissions,

•

recyclable,

•

full colour matching possible,

•

lower densities compared with EPDM.

8.2.2 Expanded (Non-Crosslinked) Polyolefin Beads An expanded polymer bead process was first developed by BASF in the 1950s for polystyrene. In the 1970s the process was extended to polyethylene and, more recently,

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Handbook of Polymer Foams to polypropylene copolymers. The production process involves converting the polymer to micropellets which are transferred to a process tank as an aqueous slurry. Here the pellets are impregnated with a hydrocarbon blowing agent such as propane at elevated temperature and pressure. After the hydrocarbon is fully absorbed, pressure is released and the particles allowed to expand to form low density beads some 4-5 mm in diameter. The blowing agent is contained and recovered for further use. Since the bead size is small and the polymer, whilst being below its melt temperature is above its glass transition, diffusion of blowing agent out of the beads is rapid and is said to be essentially complete within a few days following production. This contrasts with polystyrene which, as it is below its glass transition at normal ambient temperatures, retains the blowing agent and is transported for use in the unexpanded state. Polystyrene beads are expanded by the producer of the final product using appropriate moulds. Polyethylene or polypropylene beads are transported in the expanded state, and hence the moulding process is technically different. It has been described by Cousins and Domas (BASF) [4] and essentially involves the following stages: 1. Mould closed, locked and preheated. 2. Back pressure applied and mould filled with expanded particles. The back pressure (0.06 – 0.40 MPa) compresses the expanded particles and hence controls the weight of foam needed to fill the mould, and also the final moulded foam density. A high back pressure results in a high density of moulded foam. 3. Mould sealed and back pressure reduced. 4. Steam passed through mould to fuse particles. 5. Water passed through mould to cool moulding and then drained off. 6. Air pressure applied to loosen moulding. 7. Mould opened and moulded part ejected. 8. Mouldings stored at elevated temperature, e.g., 80 ºC, to stabilise dimensions. It will be realised that foam mouldings are inevitably denser than the nominal bulk density of the expanded particles. Some data for Neopolen P (polypropylene bead foam produced by BASF) [4] is shown in Table 8.1. Since the low bulk density of EPP particles (and the requirement to transport in the expanded state) results in high transport costs, development work has attempted to find

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bulk density Neopolen P moulded density Neopolen P Polyolefin Foams

Table 8.1 Comparison of nominal bulk density and typical moulded density for Neopolen P Nominal bulk density, kg/m3

Typical moulded density, kg/m3

11

21-26

17

26-35

28

50-65

methods of moulding lower density foams from higher density beads. A method of achieving this has been described by Cousins (BASF) [5] . In this process particles are pre-pressurised with air (0.3-0.4 MPa) at elevated temperatures (70-80 ºC) for a period of 4 to 6 hours. This technique essentially introduces air as a post-manufacture blowing agent. The pre-pressurised particles are passed into the mould as normal, but the additional blowing effect of the air allows significantly greater expansion within the mould, resulting in moulded densities comparable with the initial bulk density of the particles, as low as 11 kg/m3. Although the process is essentially a batch method, it can be operated quasi-continuously by use of a large pre-pressurising vessel in which particle levels are maintained by a small dosing feed tank and from which pressurised particles are taken as required to feed moulds. Tank volumes need to be large enough to achieve an average residence time of the required 4-6 hours. The method is described as the Pressure and Temperature System (PAT) or, in its quasicontinuous form, C-PAT. Production of EPP beads is also possible by extrusion, and in 1996 Montell introduced Higran F, an EPP bead grade based on extrusion foaming of their high melt strength Higran polypropylene. Technology is available from Berstorff and essentially involves cutting the extrudate directly at the die plate by means of a rotary knife [1]. The pellets expand due to the pressure decrease and are then cooled in a water flow prior to drying and bagging. The process can be used for both polyethylene and polypropylene bead production.

8.2.3 Extruded Crosslinked Foam - Processes There are essentially two processes for the manufacture of crosslinked polyolefin foam by extrusion. Both use a chemical blowing agent but are distinguished by the crosslinking method:

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Handbook of Polymer Foams •

Irradiation crosslinking, in which crosslinking and expansion are separate making it easier to balance the two stages of reaction

•

Chemical crosslinking, in which crosslinking chemicals are compounded into the mix at an early stage, with crosslinking taking place at the same stage as expansion. This process is more sensitive to operate owing to the additional heat input at the compounding stage and the requirement to balance crosslinking and blowing agent decomposition at the expansion stage.

Both processes were originally developed in Japan and have subsequently been commercialised worldwide. The chemical crosslinked process is the more common as it obviates the requirement of costly irradiation equipment.

8.2.3.1 Irradiation Crosslinked Extruded Sheet The process, originally developed by Sekisui Electrical Co., Japan, involves three stages; sheet extrusion, irradiation crosslinking, and expansion. In the first stage, powder grades of LDPE or EVA copolymers or blends are fed into a high length:diameter ratio (L/D) extruder, e.g., 30:1, together with a chemical blowing agent and activators, lubricants, pigments as required. A powder polymer feed is necessary to ensure good mixing and uniform feed ratio with the chemical blowing agent, which is added at typical levels of 10-20 phr. An essential requirement is to keep the melt temperature below the decomposition point of the blowing agent to prevent premature expansion in the extruder, and melt temperatures normally are maintained at 130-145 ºC which is adequate for melt fluidity without pre-decomposition. The extruder is designed to provide good mixing whilst giving good temperature control, and feeds a sheet die providing extruded sheet up to 1.5 m wide and 4 mm thick. At the end of the extruder line, the sheet is exposed to radiation. Although technically this could be from a gamma ray source (Cobalt 60), in practice electron beam radiation is used owing to the greater control, freedom from gradual decay, and no requirement for permanent heavy shielding (though some shielding is necessary). However, electron beam radiation equipment of the type which can be safely used in a normal factory environment is not as penetrating as gamma radiation and this imposes a thickness limitation on the extruded sheet (and hence expanded foam). Ideally, the induced crosslinking should be uniform through the sheet and this may be better achieved with thicker sheet by passing twice through the beam, the second time

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Polyolefin Foams the sheet being turned over. This does however interfere with process continuity and adds to cost. Radiation doses are in the range 1000-200000 Gy, depending on formulation - EVA is more sensitive to radiation requiring a lower dose for crosslinking and is usually present in the mix for this reason. Crosslink levels are substantially lower than, for example, rubber vulcanisation, with solvent extractable levels around 30-40%. Although the process is generally thought of as continuous, in practice the crosslinked sheet is stored in take up rolls until needed and then expanded as required. Extrusion crosslinking stages do not then have to match the linear throughput rate of the expansion stage and storage space requirements are reduced. Expansion is carried out in an infra red (IR) hot air oven generally arranged vertically so as to minimise the degree of contact of the hot expanding sheet with guidance bars which have to cope with the three dimensional expansion of the sheet. Temperatures are in the range 220-230 ºC. The expanded sheet is taken up on rolls. It has a fine cell structure and good surface quality, although the latter can deteriorate owing to degradation from high irradiation doses with thicker sheet. This is another factor limiting sheet thickness.

8.2.3.2 Chemically Crosslinked Extruded Sheet This process was developed independently in Japan by Furukawa Electric Co. and Hitachi Chemical Co. and, like the irradiation process, has subsequently been licensed for operation worldwide. The Furukawa and Hitachi processes are similar in the initial stages, differing at the expansion stage. The first stage involves melt compounding a peroxide crosslinking agent and a chemical blowing agent with the chosen polymer. Since both the crosslinking agent and the blowing agent will decompose or react if compounding temperatures reach critical levels for any length of time, temperatures at this stage are closely controlled and the crosslinker and blowing agent system are selected so as to give a safe operating window. The usual crosslinker is di-cumyl peroxide (DCP) which has a half life of l minute at 170 ºC and a melting point of 55-60 ºC. Dispersion is often aided by use of an inert carrier which mitigates the screw slip resulting from the presence of melted peroxide. The blowing agent is normally activated ADC formulated so no significant decomposition occurs below 120-130 ºC. However, care has to be taken to eliminate ‘dead spots’ in the mixer where material may be held up for an extended time since this can result in some premature blowing. Decomposition of the blowing agent is also dependent to some extent on particle size, and this is also controlled.

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Handbook of Polymer Foams Compounding methods include both internal Banbury type mixers feeding a pelletising line, and twin screw compounding extruders. Good dispersion is essential in achieving high quality expanded sheet with uniform cell structure. Crosslinker and blowing agent may be compounded together or as separate mixes. Compounded pellets are then fed to a sheet extruder having good mixing characteristics whilst minimising heat build up. Extruder design is critical in achieving this and more recently co-rotating twin screw extruders are receiving consideration owing to their good mixing characteristics combined with heat transfer for good cooling. Under these conditions premature crosslinking and blowing can be eliminated. These reactions are time/temperature dependent and the aim is to achieve good mixing whilst temperature does not exceed a maximum determined by the residence time in the extruder and die. In practice, temperatures are maintained at 110-120 ºC, and the main problem encountered is normally hang up of mix at elevated temperature in the die or extruder such that the theoretical residence time is significantly exceeded. This can result in crosslinked or even expanded particles in the extruded sheet which give rise to defects when the sheet is expanded. Following from these considerations, sheet die design is such as to minimise dead spots. The extruded sheet is taken up on rolls and held at least 24 hours before proceeding to the expansion stage. Some quality control tests may be carried out on the extruded sheet but these are generally restricted to a check on thickness and an inspection for obvious premature reaction of crosslinker or blowing agent. At the expansion stage, differences in the two processes become apparent: •

Furukawa process: a continuous wire mesh conveyor is used to carry the sheet through a three zone hot air oven. Heating is accomplished by hot air jets above and below the conveyor which serve also to release the sheet from the conveyor after significant crosslinking so as to allow expansion. Failure to release will result in tearing as the sheet tries to expand, such tearing and poor release often being indicative of insufficient crosslinking. Although the crosslinking step is arranged to occur at a lower temperature than blowing agent decomposition, in the Furukawa process the two processes to some extent go on concurrently. Oven temperatures are about 230 ºC. The expanded sheet passes through an edge trimmer and then via a take off system to a take off roll.

•

Hitachi process: the compounded sheet is taken by a silicone rubber/fibreglass reinforced conveyor into an infra red preheating crosslinking oven where a high degree of crosslinking is achieved prior to subsequent expansion. This level of crosslinking enables the sheet to expand totally unrestricted in the next stage which is a hot air oven. No mesh conveyor is needed. The separate crosslinking zone enables a higher level of crosslinking and lower foam densities to be achieved compared with

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Polyolefin Foams the Furukawa process. In addition, the higher melt strength which permits free expansion also gives a smoother skin with finer cells and fewer cell irregularities (voids or pinholes). A disadvantage is the necessity of maintaining tight control over the balance of crosslinking and blowing; too great a level of crosslinking restricts expansion and may cause excessive shrinkage of the expanded sheet, whilst a low crosslink level will result in a low melt strength and consequent likelihood of sheet tearing and/or cell collapse during expansion. As with the Furukawa process, expanded sheet is trimmed and taken up on a roll. Both the Hitachi and the Furukawa processes result in some surface oxidation/degradation during the high temperature expansion stage. Process modifications to minimise this have been described, e.g., use of a nitrogen blanket, but these are not known to be operated. The same applies to processes using a high temperature liquid salt bath for curing and expansion. Such a process is reported to give both good cell structure and high surface quality [6].

8.2.3.3 Materials

• Polymers Selection is made primarily on the basis of ensuring that melt processing temperatures should not exceed 120 ºC during compounding and extrusion of unexpanded sheet. Normally, LDPE and EVA, alone or as blends, are used, with melt flow indices in the region of 2.0-4.0 g/min. These polymers, particularly EVA, crosslink reasonably efficiently with peroxides and process at acceptably low temperatures. HDPE and LLDPE require higher processing temperatures and are not used. Polypropylene, whilst a desirable polymer to expand owing to its higher use temperature and generally lower cost, poses problems for crosslinked foam production due firstly to the necessarily higher processing temperature and secondly to the difficulty of crosslinking. Free radical crosslinking with peroxide normally leads to chain scission and degradation of polypropylene rather than crosslinking. Polypropylene sheet foams are therefore made using blends of suitable polypropylene copolymers, which have a lower and broader melting point and hence lower processing temperatures, together with an additive to enhance crosslinking. Various possible additives have been described in the patent literature, many of them of dubious acceptability for health and safety reasons, e.g., divinyl benzene, and manufacturers of crosslinked polypropylene foam sheet use undisclosed proprietary systems. More recently, metallocene catalysed polyethylenes (mPE) have become available. These materials can have enhanced physical properties owing to the greater regularity of chain

183

Borealis Exxon Phillips Elenac Dow Dex Plastomers Dupont Dow Handbook of Polymer Foams structure, and the catalysts allow a wide range of polymers to be produced having densities from about 0.87 to 0.94 g/cm3. Polymer flexibilities vary in line with density and at the lower end compare well with the flexibility of EVA copolymers. The availability of these materials in Europe has been reviewed by Maier [7] and is summarised in Table 8.2. Densities cover the range of medium density polyethylene (MDPE; 0.93-0.94 g/cm3), LDPE (0.915-0.935 g/cm3) and LLDPE/very low density polyethylene (VLDPE; 0.900.93 g/cm3), together with new materials having densities less than 0.90 g/cm3. A differentiation is sometimes made between polyolefin plastomers (POP), which have applications in the film and packaging area, and the newer lower density polyolefin elastomers (POE) which are now competing with thermoplastic elastomers (TPE), flexible polyvinylchloride (PVC), crosslinked elastomers, and ethylene copolymers [EVA and ethylene methyl acrylate (EMA)]. Whilst having the potential to provide improved foam properties and also foam flexibilities previously only achievable through use of copolymers such as EVA, the processing problems of metallocene polyolefins, resulting in high heat build up at the sensitive mixing and extrusion stages, has restricted the use of these materials for cross-linked foam production. When used, they are always blended with something else, e.g., LDPE.

Table 8.2 Commercial availability of mPE (Europe) Producer

Product

Co-monomer

Density range, g/cm3

Borealis

Borecene

1-hexene

0.934-0.94 0

Elite

1-octene

0.916-0.935

Exxon

Exceed

1-hexene

0.918

Phillips

mPact

1-hexene

0.916-0.933

Elenac

Luflexen

1-butene

0.903-0.917

Elenac

Luflexen

1-hexene

0.918

Dow

Affinity

1-octene

0.868-0.915

Exact

1-octene

0.90 2

Engage

1-octene

0.8863-0.910

Dow

Dex Plastomers Dupont Dow Source: [7]

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Polyolefin Foams

• Blowing Agents ADC is used as the blowing agent of choice. Decomposition is controlled by the use of activators such as zinc oxide or an organo zinc complex which may be incorporated in the material as supplied, or compounded in later as part of the mix. A further factor controlling decomposition rate and the temperature of decomposition is particle size. Fine particles decompose preferentially and thereafter catalyse the decomposition of larger particles. Manufacturers of ADC therefore use processes involving crystallisation control and air grading, aiming to produce uniform coarse particles (diameter 3 μm or less). Such materials reduce the possibility of premature decomposition during mixing and extrusion. Particle size distribution does vary between grades from different manufacturers and foam producers tend to have preferences depending on the particular process being operated. The electron beam process, which separates the crosslinking and expansion stages, can tolerate a somewhat wider particle size distribution than the chemical crosslinking processes.

• Crosslinking Agent The requirement of the crosslinking agent is to remain inactive during compounding and extrusion (some 5 minutes at 120 ºC), with rapid crosslinking triggered subsequently at higher temperatures before any substantial decomposition of blowing agent. Alkyl peroxides are most commonly used, usually dicumyl peroxide (half life 1 minute at 171 ºC). If a higher decomposition temperature is needed, then 1, 3-bis (t-butyl peroxy iso propyl) benzene is an alternative (half life 1 minute at 182 ºC). Silane crosslinking has been described [8] and is in limited commercial use. Silane groups are grafted on to the polymer during compounding and crosslinking is effected after extrusion by exposure to moisture (or steam). The process eliminates the possibility of premature crosslinking in the extruder (provided polymers are dry) but imposes a thickness limitation owing to the exposure time necessary to allow diffusion of moisture into the foam, which increases as the square of extrudate thickness.

• Other Additives Antioxidants and UV stabilisers are not normally added to formulations. LDPE grades used are free from antioxidants (although EVA grades normally have low antioxidant levels as supplied). Although such additives could reduce surface oxidation at the high

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Handbook of Polymer Foams temperature oven expansion stage, they interfere with peroxide crosslinking. Microcrystalline additives such as talc have been mentioned in the literature as cell nucleators but are not normally used. Process aids such as zinc stearate may be added, but these are also activators for the blowing agent, which must be allowed for. Crosslinking aids, in the form of small amounts of EVA or acrylate terpolymers, may be used but have an effect on foam flexibility. Pigments are commonly added to produce coloured foams. Pigment masterbatches aid dispersion with minimum shear (and heat build up) and give a cleaner working environment. It should be noted that no pigments are needed to produce white foams, since the multitudinous reflections from cell walls gives foams a naturally white appearance. It may however be necessary to use white pigments (titanium dioxide) in combination with coloured pigments if pale pastel colours are required. Flame retardants are added to produce flame resistant foams, antimony trioxide/halogen systems being the most effective. Like pigments, these are added as masterbatches. Typical Formulations are, for 100 parts polymer: 5 phr ADC and 0.5 phr DCP to give foam density 100 kg/m3 10 phr ADC and 0.7 phr DCP to give foam density 60 kg/m3 17 phr ADC and 0.9 phr DCP to give foam density 30 kg/m3 Further information on the Sekisui, Furukawa and Hitachi processes can be found in reference [6].

8.2.4 Press Moulded Crosslinked Foam Process The semi-continuous nature of the crosslinked sheet foam process gives good production efficiency but both the radiation and chemical crosslink routes have a limitation on the maximum thickness of foam that can be produced. In the radiation process it is the inability of the electron beam to achieve uniform crosslinking with thick extrusions, whilst in chemically crosslinked foam the limitation is heat transfer at the crosslinking/ expansion stage. Normal maximum thickness of extruded crosslinked sheet foam is about 15 mm. (The nitrogen autoclave process described later can produce ‘thin blocks’ up to about 50 mm). Whilst thicker foams can be produced from thin sheet by heat lamination, problems can arise due to surface degradation at the expansion stage and lamination quality is poor unless a surface skin is removed beforehand.

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Polyolefin Foams Hence, thick foams (up to 120 mm) are made by press moulding or injection moulding methods whereby crosslinking and blowing agent decomposition are carried out in a closed mould. Expansion occurs subsequently. Note: injection moulding is generally limited to production of foam densities greater than 100 kg/m3. Several variations of the press moulded process are in commercial use, and are discussed in Sections 8.2.4.1 and 8.2.4.2

8.2.4.1 Single Stage Process Closely related to the methods used for the production of closed cell elastomeric and flexible PVC foams, the process involves firstly compounding the polymer with crosslinker, blowing agent and any required additives. As with crosslinked sheet foam, care must be taken to minimise heat build up so as to avoid premature crosslinking and blowing. Banbury batch mixers and twin screw compounding extruders are both used. A defined weight of compound is then placed in a mould and press cured, typically for 45 minutes at 150 – 170 ºC. Under these conditions curing is complete and the blowing agent is fully decomposed. When the mould is opened the product expands directly, literally jumping out of the mould. Moulds are designed to facilitate this. Whilst having the advantage of simplicity, the single stage process has several disadvantages, namely: •

High mould pressures are generated, particularly at low foam densities which use formulations with greater amounts of blowing agent generating larger gas volumes for greater expansion. This requires the use of heavy duty presses and high clamping forces.

•

Only a part of the platen area can be used so as to avoid contact of the expanding foam with the guide pillars, with consequent foam distortion.

•

High press opening speeds are necessary (> 10 cm/s) to accommodate the rapid foam expansion.

Mould design is critical to avoid generation of internal stresses with the likelihood of foam defects during expansion.

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Handbook of Polymer Foams For these reasons foam density is restricted to a minimum of 70 kg/m3 with the single stage process, higher degrees of expansion requiring a two stage process.

8.2.4.2 Two Stage Process Compounding is carried out as for the single stage process, but at the press curing stage crosslinking and gas evolution are controlled to ensure no or only partial expansion occurs on release from the mould. Full expansion is carried out in a later second stage. Several variants are operated, including: •

Press curing for some 40 minutes at 130 ºC. The product is essentially fully crosslinked but there is only partial decomposition of the blowing agent and therefore only limited expansion from the mould. The expansion is completed by transferring the product to a hot air oven, typically for 50 minutes at 170 ºC.

•

Press curing for some 20 minutes at 130 ºC, resulting in partial curing but no significant decomposition of blowing agent. The product is taken from the mould and transferred to a hot air oven as before to complete curing and enable expansion, typically 60 minutes at 165 ºC.

Press curing at 170 ºC followed by chilling. Curing is complete and most of the blowing agent is decomposed. Chilling the product (before the mould is opened) gives the material sufficient strength to prevent significant expansion after removal from the mould. Whilst immediate transfer to an expansion oven is not necessary, there is a slow loss of the blowing agent trapped at high pressure within the solid product, and final expansion is generally carried out shortly after press curing, again in a hot air oven. In all these two stage processes, product from the first stage can be transferred to an expansion mould for the second stage, in which case heating can be carried out using steam. An expansion mould allows final dimensions (and hence foam density) to be closely defined. Formulations for press moulding are not so critical as those for crosslinked extruded foam since it is not so essential to achieve a balance between crosslinking and blowing agent decomposition. However, the same requirements exist regarding choice of these additives, and ADC together with DCP crosslinker are the agents of choice. Polymers are LDPE/EVA blends with zinc oxide activator and stearic acid processing aid. A typical formulation is shown in Table 8.3. Pigments and flame retardants may be incorporated to give coloured or flame resistant foams and generally also improve cell structure by also acting as nucleating agents.

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press moulding Polyolefin foams Polyolefin Foams

Table 8.3 A typical formulation for press moulding Ingredient

Quantity

LDPE

100 phr

EVA

15 phr

DCP

2.1 phr

AZDC

6.0 phr

Zinc oxide

2.0 phr

Stearic acid

1.0 phr

Source: [9]

8.2.5 Injection Moulded Foam Process Polymers are selected to have high melt fluidity in the range 100 – 120 ºC so as to permit good mixing without predecomposition. Screws with high L/D ratio (25 – 30:1) are used for mixing prior to injection, and formulations are similar to those used for press curing. During moulding, similar constraints apply as for the single stage process since the product expands directly from the mould, with mould design important in preventing undue internal stress during expansion. Mould temperatures are about 200 ºC and insulation is needed to maintain temperature uniformity (and hence uniformity of crosslinking and expansion within the product). Foam densities are normally in the range 100 - 300 kg/m3. Press curing processes have been reviewed by Puri and Collington [9].

8.2.6 The Nitrogen Autoclave Process This is a unique process operated by only one company worldwide (Zotefoams plc, Croydon, UK). The process was originally developed in the late 1950s and was commercialised in the early 1960s. It comprises three stages, namely: •

Extrusion and crosslinking

•

High pressure gassing

•

Low pressure expansion

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8.2.6.1 Stage 1 At the first stage a polyolefin together with a crosslinking agent and any other desired additives such as pigments and flame retardants is extruded using an extruder with good mixing ability. Originally single screw extruders with high L/D (25 - 30:1) and appropriate mixing sections were used; more recently co-rotating twin screw compounding extruders have been introduced. The mix is fed to an extrusion die to produce sheet up to some 12 mm in thickness. Extruded sheet is carried on a conveyor belt (coated with fluoropolymer for good heat resistance and to avoid sheet sticking) into a curing oven where the temperature is held at some 160 ºC over a residence time of about 20 minutes to achieve complete curing. Since there is no blowing agent incorporated at this stage the problem of balancing crosslinking and blowing reactions is eliminated, though care must be taken to avoid premature crosslinking. A peroxide crosslinker is used having a somewhat higher decomposition temperature than DCP at levels very much lower than those used in other chemically crosslinked foam systems. This reflects the higher molecular weight polymers used (resulting in improved foam properties) and the lower crosslink level needed to stabilise the foam during expansion. Polymers used are HDPE, LDPE, EVA, EMA, polypropylene, metallocene polyolefins, and various blends of these materials. After exiting the crosslinking oven, the extruded sheet is cooled and cut to precisely sized polymer slabs. These are quite stable and may be stored indefinitely until required for expansion. When first developed the process did not use chemical crosslinking. Cut slabs were crosslinked after the extrusion stage by radiation in a separate operation. This option, although more costly, is still used for polymers which have too high a processing temperature to allow incorporation of peroxide without premature decomposition. This includes HDPE, where slabs are cured off site either by cobalt 60 gamma radiation or electron beam irradiation. The radiation sources are more penetrative than would be possible in a normal factory environment and the thickness limitations of the Sekisui process do not apply. An irradiation regime is used whereby slabs are turned and interchanged to ensure uniform crosslinking through each slab. Since slabs can be sampled after crosslinking, quality controls can be introduced to ensure the process is operating within specified tolerances. As well as slab dimensions this check includes measuring crosslink level which is not possible with other processes. Any deviations can be corrected by minor adjustments of crosslinker at the extruder.

8.2.6.2 Stage 2 At the second stage the blowing agent is incorporated. This is pure nitrogen which is dissolved in the slabs by exposure to the gas at high pressure (up to 70 MPa) and

190

Polyolefin Foams temperature (above the melting point of the polymer, typically 150 ºC. Under these conditions, despite the low solubility of nitrogen in polyolefins, sufficient gas dissolves to ensure subsequent expansion. The amount of gas dissolved, and hence the degree of subsequent expansion depends on temperature and more particularly, pressure. Final foam density is determined at this stage, and foams having densities over a wide range (commercially 15 to 120 kg/m3) are made from a single formulation by varying the pressure in the high pressure autoclave. Temperature/pressure cycles must be sufficient to ensure complete dissolution of gas. This is a diffusion process dependent on temperature, pressure and slab thickness, and times are typically 6-8 hours to achieve saturation. Foam quality can deteriorate if there is any oxygen present as an impurity in the nitrogen and through any temperature non-uniformity. Measures are taken in gas supply and autoclave design to minimise these factors. After the slabs are saturated with nitrogen, gas pressure is reduced and the slabs cooled. Gas comes out of solution causing cell nucleation but no significant expansion takes place at this point. Cooling continues until the slabs have sufficient solid strength to contain the trapped nitrogen without expansion, whereupon the pressure is reduced to zero gauge and the slabs removed from the autoclave. The pressure cycle in the autoclave controls cell size. A fast reduction in pressure after saturation increases the cell nucleation rate, resulting in a greater number of cells in the expanded foam with consequently smaller diameter. Slower rates of pressure reduction result in larger cells. Cell diameters are controlled within the range 0.1-1.0 mm.

8.2.6.3 Stage 3 The final expansion stage is carried out within a few hours of gassing to avoid any significant loss of gas from the slabs. Expansion is done in a low pressure autoclave of sufficient size to accommodate full expansion of the foam blocks. Air pressure is applied (approximately 1.5 MPa) and the temperature raised above the polymer softening point to about 150 ºC. When the slabs have reached this temperature the pressure is released to allow rapid expansion providing foam blocks up to 2 m x 1 m in length x width and up to 50 mm in thickness. Whilst it would be possible to expand in an air oven, the use of a pressurised vessel, by preventing expansion until the slabs are at uniform temperature, enables controlled expansion with no internal stress and hence improved foam quality.

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Handbook of Polymer Foams Capital cost of the autoclave process is substantially more than that of other processes, due mainly to the cost of the high pressure autoclave and ancillary equipment. The design of the autoclave, including the closure which allows for easy insertion and removal of extruded slabs whilst maintaining the necessary high pressures during the process cycle, is proprietary to Zotefoams as are the detailed operating parameters. Running costs can nevertheless be lower than other processes owing to the high productivity of a high pressure autoclave for the production of low density foam, and the absence of any costly blowing agent. Advantages of the autoclave process are: •

The blowing agent, pure nitrogen gas, leaves no solid residues in the foam. Such residues can reach significant levels in foam expanded with chemical blowing agents and are a major limitation in production of such foams at densities less than some 25 kg/m3. The autoclave process does not have this limitation and foams are produced down to 15 kg/m3 commercially and 10 kg/m3 foams have been made in development work.

•

Crosslinking and expansion are separated, simplifying production, enabling quality control measures to be introduced at intermediate stages and widening the choice of suitable polymers. The option of irradiation crosslinking enables manufacture of foams using polymers having high processing temperatures such as HDPE.

•

Cell size is under control at the high pressure second stage. Crosslinked slabs may be expanded in a range of cell sizes and this choice does not have to be made until the foam is expanded.

•

Foam cell structure, i.e., the uniformity and integrity of the cells, is significantly better than that found with other processes, leading to property benefits, particularly in strength and compression set.

A disadvantage is the high capital cost and it is this, together with the undisclosed proprietary operating parameters, which have prevented this technology from becoming more widely adopted. However, Zotefoams have recently entered into a sales alliance with Alveo (who produce extruded sheet and block foam), and are also building a manufacturing plant in North America, so the technology may be starting to disseminate. Interestingly, the North American plant will operate initially by expansion of gassed slabs produced by the UK plant and shipped over in refrigerated containers. This reduces the transport costs of shipping expanded foam and eliminates for a time the cost of a high pressure autoclave at the new site. Some further information on the autoclave process is given in references [10], [11] and [12].

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Polyolefin Foams

8.2.7 Recycling Processes Non-crosslinked polyolefin foams can be readily recycled by granulation and extrusion. The recycled product may be incorporated with virgin polymer at levels of 10 - 20% to produce new foam with little effect on foam properties. The main difficulty, as with many recycling operations, is that of segregation and collection of foam for recycling without contamination, e.g., by other foams which may not be easy to identify. Within the manufacturing operation this problem can be solved by careful control of reject material and trimmings, but there is a considerable problem in ensuring foam consumer waste is free from contamination. Some foam manufacturers in response, for instance, to packaging waste legislation, have set up schemes whereby foam can be segregated, collected and returned to the production unit for recovery. Crosslinked foam cannot easily be recovered and used for new foam production since the crosslinks interfere with melt flow. Other recycling methods have therefore been developed: •

Reuse is emphasised, the crosslinks being beneficial in establishing and maintaining good properties. Crosslinked polyethylene foam is the material of choice for reusable packaging, for example as in house transit packs for automotive parts.

•

Coarsely chopped foam may be heat moulded to form, e.g., drainage liners for rooftop gardens. The granules (10 - 20 mm in size) are transported on a conveyor through a heating chamber and are then consolidated by shaped rollers or in a press.

•

More finely chopped foam (5 - 10 mm in size) can be consolidated by equipment in which foam granules are passed between a rotating and a stationary plate. Granules become heated above the melt point by shear effects and the foam structure is destroyed. The consolidated granules can be used as a coarse moulding powder although the original objective of this process was density increase to reduce waste volume. A foam of density 50 kg/m3 can increase in density to some 400 kg/m3.

•

Many regard energy recovery as the best option for recycling plastics although this is not encouraged by, for example, the European Packaging Regulations. Polyethylene can be combusted to produce energy with an effectiveness some 3 times that of cellulosic products, e.g., paper, cardboard, wood, with no possible evolution of noxious halogen or nitrogen compounds. Domestic waste can be difficult to combust without the presence of waste polyethylene.

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8.2.8 Post Manufacturing Operations Polyolefin foam is normally an intermediate material which has to undergo further processes to give a final product. Such processes may include: Sawing Splitting Die stamping Hot wire cutting Laminating Butt welding Thermoforming

Adhesive bonding Routing Sanding Drilling Flocking Printing

The surface of polyethylene foam is non-polar and has a low level of interaction with surface treatments such as flocking, printing and adhesive bonding. Such treatment generally requires special formulations or a surface pre-treatment to ensure success. Copolymer foam such as EVA is more amenable to these processes as this is more polar. Sheet lamination to build up thick blocks from two or more sheets does not require adhesive as the surfaces will self-bond if heated above the polymer melting point. The original sheet surface, which may be rough and degraded through oxidative reactions during the high temperature stages of production, is often split off prior to lamination. Surfaces are heated by hot air or, preferably, by passing over a heated blade (the latter technique gives greater temperature uniformity) and then brought together immediately after the hot zone. The bond formed is at least as strong as the foam. Laminates having more than two sheets are preferably built up symmetrically to avoid distortion (curvature) caused by minor differences in compression imposed by top and bottom feed rollers. Butt welding is carried out using analogous techniques to heat lamination. Several different methods are in use for thermoforming which, in contrast to heat lamination, can only easily be carried out with crosslinked foams. Whilst thermoforming of solid materials is precluded by the presence of crosslinks, in polyolefin foams a small amount of crosslinking stabilises the cell structure in the hot state and the moulded form is retained by the strength of the polymer below its softening point. The methods in use are: •

Heat moulding: foam is placed in a mould with an overload of some 10%. The mould is closed, heated to a temperature above the softening point of the polymer, e.g., for polyethylene foams, 140-150 ºC, and then cooled. The moulded product is removed from the cold mould.

194

Polyolefin Foams •

Heat impression moulding: foam sheets cut to the appropriate size are placed in an infra red oven for a time dependent on sheet thickness and density, e.g., for LDPE foam of 45 kg/m3 density, Zotefoams recommend 10 seconds heating at 140 ºC per 1 mm thickness of foam. The hot sheet is transferred to a cold mould and pressed for a similar time to that used for heating. The method is faster and cheaper than heat moulding but makes considerable demands of foam hot strength for low density foams and/or high draw ratios. Better thermoforming is found with higher density foams having intrinsically greater hot strength.

•

Vacuum forming: the foam is heated as for heat impression moulding and then transferred to a one piece mould with provision for the application of vacuum to draw the foam down to the mould shape.

•

Body forming: in an interesting variant used for medical applications hot sheet is wrapped around the human body to produce wrist, ankle, knee and other supports which conform precisely to the body shape. Although the foam is heated to 140 ºC, the low heat content and thermal conductivity allow this to be carried out without any discomfort to the patient.

8.3 Properties of Polyolefin Foams As with all foams, properties depend on the following factors: •

Type of polymer

•

Closed cell versus open cell content

•

Foam density

•

Presence of any modifying additives

•

Cell structure and integrity

Polyolefin foams are almost wholly closed cell and modifying additives are mostly restricted to small amounts of pigments, nucleating agents and processing aids, none of which have any significant effect on properties. Flame retardants, however, are added at levels up to 20% by weight and can affect physical properties in addition to conferring flame resistance. Fillers are not normally used since they increase density without any positive contribution to physical properties. In general, therefore, physical properties depend on polymer, foam density and cell structure. The effect of foam density on properties is shown in Table 8.4 for a range of LDPE based foams.

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Zotefoams plc Handbook of Polymer Foams

Table 8.4 Effect of foam density on properties (autoclave process) Formulation 1

2

3

4

5

Foam density (kg/m3)

24

33

45

60

70

Compression strength 25% (kPa)

35

40

50

70

85

Compression set (%) 1

32

27

22

19

16

Tear strength (N/m)

410

690

1130

1490

1855

Tensile strength (kPa)

340

455

600

790

945

Elongation at break (%)

105

135

150

160

170

Flexural modulus (MPa)

0. 4

0.7

1.0

1.7

2.7

Note 1: 72 h at 50% compression, 0.5 h recovery Source: Zotefoams plc, data sheets

As may be expected, all properties improve as foam density increases. The effect that choice of polymer has on properties is shown in Table 8.5, comparing foams of similar densities. The increase in maximum use temperature is evident in moving from ethylene copolymers to homopolymers, reflecting the higher softening point. The greater elongation and flexibility of the copolymer is also shown. Highest strength is found with high density polyethylene foams, making these materials very tough and suitable for applications in areas of high impact stresses. Some data on the effect of foam structure has been given in [12]. Foams made using chemical blowing agents are shown to have a more poorly defined cell structure which is considered to relate to the lower physical properties measured, e.g., tensile strength 45% lower, elongation at break 30% lower, and compression set up to 3 times greater compared with autoclave foams. Some data has been published on autoclave foams produced using metallocene polyolefins [11, 12]. Compared with LDPE foams of the same density and similar flexural quantities, metallocene foams have approximately 60% higher tensile strength, 55% higher

196

Zotefoams plc Polyolefin Foams

Table 8.5 Effect of polymer type on properties (autoclave process) Polymer type EVA

LDPE

HDPE

Foam density (kg/m3)

35

33

30

Maximum use temp. (ºC)

80

105

125

Compression strength 25% (kPa)

35

40

60

Compression set (%) 1

33

27

22

Tear strength (N/m)

730

690

1320

Tensile strength (kPa)

620

455

825

Elongation at break (%)

200

135

55

Note 1: 72 h at 50% compression, 0.5 h recovery Source: Zotefoams plc, data sheets

elongation at break and more than double the tear strength, making these materials particularly suitable for applications involving hard wear.

8.4 Applications Polyolefin foams have an extremely diverse range of applications and there are few, if any, industries where these foams are not used. Some of these areas, and specific applications, are listed: •

Appliances

Gaskets and vibration pads: foam densities from 15 to 60 kg/m3, using LDPE or EVA, depending on the particular performance requirements. EVA foam has greater flexibility and compression recovery whilst LDPE has better load bearing capability. •

Automotive

Gaskets and seals; water barriers; carpet underlay; sound insulation; vibration pads; headliners; impact protection. LDPE foams in densities from 15 to 45 kg/m3 are generally used, with EVA and EMA foams having application where greater flexibility is needed,

197

Handbook of Polymer Foams e.g., gaskets, carpet underlay. HDPE foams have a use where high impact protection is needed. Polypropylene copolymer foam sheet, with higher temperature resistance up to 130 ºC, also has a wide application, and recent low density (15 kg/m3) metallocene foams are also being promoted as they offer good properties with weight saving. Polypropylene bead foam is widely used in impact absorbing bumpers. •

Building and Construction

Sealing backers; expansion joints; glazing seals; eaves fillers; impact sound absorption; pipe insulation. LDPE and EVA foams in a range of densities from 15 to 50 kg/m3 are used, with the higher densities required particularly where load support is needed, e.g., under floor blocks providing impact sound absorption. Flame retardant grades are used where appropriate in conformity with building regulations. •

Aerospace

Sealing; flotation cushions; sound insulation; ducting lining. An important criteria for almost all aerospace applications is flame retardance to Civil Aviation Authority (CAA) 8 (UK) [13] or Federal Aviation Authority (FAA), Federal Aviation Regulations (FAR) (USA) standards which involves a vertical burn test for flammability. Airbus have additional requirements involving smoke and toxicity. LDPE foams with densities up to 50 kg/m3 are in use but lower density foams are preferred (for weight saving reasons) where these are capable of meeting physical property requirements. Zotefoams’s very low density (15 kg/m3) flame resistant foam based on metallocene polyethylene is specifically targeted at aerospace applications. •

Marine

Life jackets; life buoys; fenders; oil booms; floating hoses. Foams used for these applications are normally LDPE based with densities up to 60 kg/m3. Lower density foams have slightly greater buoyancy but lower physical properties and are only used where cost is an important consideration. In some applications, e.g., fenders and floating hose, the foam is coated with one or more layers of protective skin, for instance polyurethane, in order to give a surface resistant to impact which could damage unprotected foam. In the case of floating hose, the ability to withstand and recover from the compression resulting from occasional deep immersion is important. •

Medical and Health Care

Splinting; cervical collars; orthopaedic shoe insoles; exercise mats; implement handles; orthotic supports. Foams used cover the whole range of densities and polymers, choice

198

Polyolefin Foams being dependent on degree of support needed (high foam stiffness) or comfort requirement (soft flexible foams). Thermoforming is frequently used, including direct forming on the body, to produce the desired shape. •

Sports and Leisure

Buoyancy aids; swim vests; kickboards; pool games; camping mats; waterslide mats; backpack inserts; sports shoe insoles; body protection; canoe seats; toys and games; sports mats; helmet liners; surf boards. As with medical applications, a wide variety of polymers and foam densities are used depending on specific application requirements. •

Electronics

Static dissipative packaging; pin insertion packs; conductive cushion packaging; Faraday cage shielding; work station mats; tote box liners; conductive shoe insoles. All these applications aim to prevent damage to sensitive electronic components by safeguarding against the effects of static discharge. Foam may be LDPE or EVA based and are made static dissipative or conductive by the addition of high structure (conducting) carbon black. Relatively high amounts (10-20% phr) are needed to give the required level of conductivity owing to the low density of the foam. Conductive foams have volume resistivity typically 5 x 103 Ω cm whilst static dissipative foams have surface resistivities typically 1 x 107 Ω/sq. ‘Antistatic’ foams are also available, typically with surface resistivities of 1 x 1011 Ω/sq. These foams, often coloured pink for identification purposes, are made by incorporation of a partially soluble antistatic agent which diffuses to surfaces and picks up moisture to form a dissipative surface layer. The product is widely used but has the disadvantage of performing poorly in dry environments. •

Military

Sleeping mats; missile packaging; weapons packaging; helmet liners; trauma padding; riot shields. High quality, tear resistant, puncture proof sleeping mats are produced using EVA foams. Packaging applications normally use LDPE foams, as do trauma padding and helmet liners. An interesting application is HDPE foam at high density (115 kg/m3) as an helmet liner in a military helmet designed to protect the wearer from a rifle shot. •

Packaging

Corner pads; case inserts; display packaging; cushion packaging. Some of these applications are relatively undemanding and cost/appearance are the major criteria. Cushion packaging however calls upon the foam to provide a consistent level of protection in packages designed for a particular load and fragility.

199

Handbook of Polymer Foams The mechanism of shock protection is impact absorption by plastic deformation of cell walls when the foam is compressed rapidly. The more rigid foams, or foams with poor cell structure allowing viscous movement of air between the cells, can give good shock absorption on first impact but high compression set results in poor performance on multiple impacts. Flexible foams absorb energy mainly by elastic compression of air in the cells and deformation of cell walls and do not give a good packaging performance even on first impact. Best results are obtained with semi rigid foams based on LDPE or (better) LDPE/HDPE blends. These give good first impact shock absorption and recover sufficiently after compression to retain a good performance over multiple impacts. The principles of cushion packaging have been described [14]. Essentially, cushion curves are generated which show the behaviour of foams of different thicknesses when subjected to impact over a range of drop heights and impact weights. Peak deceleration (G) is plotted against static stress to generate a series of parabolic curves. Packaging is designed so that the expected impact occurs near the trough of the curve, i.e., the lowest peak deceleration. Foam manufacturers supply data for their products both in graphical form and as software packages which facilitate the selection of appropriate foam density and thickness. Both crosslinked and non-crosslinked foams are used for cushion packaging with better multi-impact performance from crosslinked foams.

8.5 Foam Specifications Some applications require foam to meet widely recognised specifications as a prerequisite of use. A number of those frequently encountered are:

8.5.1 Packaging •

AA-59135 and AA-59136 [15, 16], Gives cushioning, i.e., impact, requirements of foams for a range of weights, drop heights, etc.

•

DEFSTAN 81-116.2 [17]and 93-101.2 [18], Impact requirements for military packaging, covering two types, i.e., GP - general purpose, and QX - explosive compatible. The latter requires certified analysis for impurity level.

•

UK/SC37767B, military specification for sleeping mats.

•

UK/SC4797B, military specification for trauma lining (of combat helmet).

200

Polyolefin Foams •

CONEG, Packaging and Packaging Waste Directive 94/62/EC [19], UK Packaging (Essential Requirements) Regulations 1998. All this legislation specifies maximum levels of lead, cadmium, mercury and hexavalent chromium in packaging. Levels started at 600 ppm reducing to 100 ppm after 30th June 2001.

•

Quality Standard BS EN ISO 9001 [20]. Whilst this is a site manufacturing standard rather than a foam specification, it is often a customer requirement and most foam manufacturers comply. Equivalent environmental and safety standards are likely to be future customer requirements.

8.5.2 Automotive FMVSS.302 [21], flammability requirement. VW/Audi fogging test; requirement for low fogging, i.e., release of organic vapours which deposit on and obscure windscreens.

8.5.3 Furnishings S1 1324 (1988) [22] as amended by S1 2358 (1989) [23]. Flammability requirement for furnishing which in the case of polyolefin foam is stated as BS 5852 [24] ignition source 2 with an FR cover fabric. Some foams meet this test without FR additives.

8.5.4 Buoyancy SOLAS [25] specifies foam requirements after temperature cycling, water absorption and diesel fuel immersion. BS EN 393 [26], 395 [27], 396 [28] and 399 [29], specify foam requirements for life jackets. Includes buoyancy test after compression underwater, and a thermal stability test.

8.5.5 Aerospace CAA 8 [13], FAA FAR 25.853 [30], JAA JAR 25.853 [31].These are the UK, USA, and joint versions, respectively, of the vertical burn test for flammability assessment.

201

Handbook of Polymer Foams ABD 0031 [32] an Airbus specification which adds smoke and toxicity testing to the CAA 8 [13] assessment.

8.5.6 Construction UL94 [33], USA Underwriters Laboratory horizontal burning test for plastic materials which includes foam in Section 12. Materials are ignited in a horizontal orientation, and assessment includes burn rate and presence of any burning drips. DIN 4102 (B1/B2) [34], German test for building construction materials. The B2 test is a vertical burn carried out on a single sample, whilst the more demanding B1 test involves a vertical chimney with test material on all four sides. An assessment is made of residual material after ignition and burning, and also temperature of the effluent gases.

8.5.7 Toys EN 71 [35], this is a wide ranging standard for toys in which part 3, covering toxicity, applies to foam as manufactured. Other parts refer to the formed final product. Maximum levels of eight soluble metals are specified.

8.5.8 Food contact FDA 21 CFR 177.1520 [36] refers to allowable substances for formulations including foams. Article 2, 90/128/EEC [37] specifies global migration limits after 10 days at 40 ºC in contact with a food simulant. These include olive oil and three aqueous types.

8.6 Markets The market for thermoplastic foams (polystyrene, polyolefin and PVC) is dominated by polystyrene which has applications mainly in building and construction and packaging. Polyolefin foams have applications in both these areas, together with many others as indicated, but tend to be used in niches where requirements are more technically or physically demanding. Total market is about 10% that for polystyrene. Some figures for annual demand of polyolefin foams published by Chemical Market Resources [38] are shown in Table 8.6.

202

annual demand Polyolefin foams Polyolefin Foams

Table 8.6 Annual demand for polyolefin foams, 1997 Country

Demand, ktonnes

North America

124

Japan

73

Western Europe

55

Growth was estimated as 4.8% annually. Since, compared with polystyrene, polyolefin foam is a relatively young product with new products and new applications continuing to arise, market growth may be expected to continue for some time. Some further information is included in reference [39].

References 1.

Film, Profiles, Beads, Tubes: XE Schaumex and Schaumtandex Lines, Berstorff, Hannover, Germany, 1998

2.

M. Van Calster, Proceedings of Foamplas ‘97 Conference, Mainz, Germany, p.149.

3.

M.H. Mack and J. Meyke, Proceedings of Polyolefins X Conference, Houston, TX, USA, 1997, p.359.

4.

J.R. Cousins and F. Domas, Proceedings of Cellular Polymers Conference, London, UK, 1991, Paper No.34.

5.

J.R. Cousins, Proceedings of Cellular Polymers II Conference, Edinburgh, UK, 1993, Paper No.29.

6.

R.R. Puri and K.T. Collington, Cellular Polymers, 1988, 7, 1, 56.

7.

R.D. Maier, Kunststoffe Plast Europe, 1999, 89, 3, 45.

8.

K.L. Walton and S.V. Karande, Proceedings of SPE Antec ‘97 Conference, Toronto, Canada, Volume 3, p.3250.

9.

R.R. Puri and K.T. Collington, Cellular Polymers, 1988, 7, 3, 219.

203

Handbook of Polymer Foams 10. D.E. Eaves, Cellular Polymers, 1988, 7, 4, 297. 11. D.E. Eaves, Proceedings of New Plastics ‘98 Conference, London, UK, 1998, Paper No.20. 12. D.E. Eaves and N. Witten, Proceedings of SPE Antec ‘98 Conference, Atlanta, GA, 1998, Volume 2, p1842. 13. The Vertical Burn Test, Civil Aviation Authority Specification No.8, 1974. 14. Cushion Packaging Guide, published by Zotefoams plc 15. AA-59135, Packaging Material, Sheet, 1997. 16. AA-59136, Cushioning Material, Packaging, Closed Cell Foam Plank, 1997. 17. DEFSTAN 81-116/2, Expanded Polyethylene Sheet – Types GP and QX – Grades A, B, C and D, 1999. 18. DEFSTAN 93-101.2, Expanded Polyethylene Sheet – Hight Density for General Purpose, 1999. 19. 94/62/EC, European Parliament and Council Directive, 1994/62/EC of 20th December 1994 on Packaging and Packaging Waste, 1994. 20. BS EN ISO 9001, Quality Management Systems – Requirements, 2000. 21. FMVSS 302, Flammability of Interior Materials – Passenger Cars, Multipurpose Passenger Vehicles, Trucks, and Buses, 1972. 22. SI 1324, The Furniture and Furnishings (Fire) (Safety) Regulations, 1988. 23. SI 2358, The Furniture and Furnishings (Fire) (Safety) (Amendment) Regulations, 1989. 24. BS 5852, Methods of Test for Assessment of the Ignitability of Upholstered Seating by Smouldering and Flaming Ignition Sources, 1990. 25. SOLAS, International Convention for Safety of Life at Sea. 26. BS EN 393, Lifejackets and Personal Buoyancy Aids – Buoyancy Aids – 50N, 1994. 27. BS EN 395, Lifejackets and Personal Buoyancy Aids – Lifejackets – 100N, 1995.

204

Polyolefin Foams 28. BS EN 396, Lifejackets and Personal Buoyancy Aids – Lifejackets – 150N, 1994. 29. BS EN 399, Lifejackets and Personal Buoyancy Aids – Lifejackets – 275N, 1994. 30. FAR 25.853, Requirements for Compartment Interiors: Crew and Passengers. 31. JAR-25.853, Joint Aviation Requirements for Large Aeroplanes: Compartment Interiors, Joint Aviation Authorities, Hoofddorp, The Netherlands. 32. ABD 0031, Smoke and Toxicity Test. 33. UL94, Tests for Flammability of Plastic Materials for Parts in Devices and Appliances, 2001. 34. DIN 4102, Fire Behaviour of Building Materials and Building Components, 1977. 35. EN 71, Safety of Toys, 1998. 36. FDA Title 21: Food and Drugs, CFR 177.1520, Indirect Food Additives: Polymers – Olefin Polymers, 2002. 37. 90/128/EC, European Commission Directive, 1990/128/EEC of 23rd February 1990 Relating to Plastic Materials and Articles Intended to come into Contact with Foodstuffs, 1990. 38. W. Dihau, Rubber World, 1998, 218, 6, 17. 39. D.E. Eaves, Polymer Foams, Trends in Use and Technology, RAPRA Technology, Shawbury, Shrewsbury, UK, 2001.

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Handbook of Polymer Foams

206

Latex Foam

9

Latex Foam Rani Joseph

9.1 Introduction Cushionable materials for upholstery, mattresses, etc., have become an indispensable component of everyday life. Such materials are known as cellular materials because they are made by providing tiny air cells in a soft matrix such as rubber or plastic. Rubberbased cellular materials can be made from both dry rubber and rubber latex. Latexbased cellular material known as latex foam is the topic of this chapter. The number of air cells, their average size and whether the cells are intercommunicating, partially intercommunicating or non-intercommunicating determine the properties of latex foam rubber such as density, cushionability, water absorption, etc. In the case of latex foam the cells are mostly intercommunicating. In 1930 a patent was granted for a process which involved mechanical agitation or whipping of latex into a foam in the presence of additives like soap, gelatin and so on [1] which assist the foaming process. This led to the production of latex foam by the Dunlop process in the early 1930s [2]. The essential feature of the process was that after foaming the latex it could be set using sodium silicofluoride, a delayed action gelling agent. The product after gelling could be vulcanised in a steam chamber [3, 4]. By 1936, several alternative methods had been proposed for the production of latex foam but none of them except the Talalay process [5] was successful. This process originally involved adding hydrogen peroxide or a low boiling organic solvent to the compounded latex and then subjecting the compound to reduced pressure for foaming. This was the forerunner of the current Talalay process, which became the only commercially important alternative to the Dunlop process. Initially foam rubber was made using natural rubber field latex but the product had disadvantages such as high shrinkage, bad odour and poor ageing resistance. There was a scarcity of natural rubber (NR) latex in the United Kingdom and North America for the commercial production of foam during the period immediately following the Second World War, so during this period the use of synthetic latices like styrene-butadiene rubber

207

Handbook of Polymer Foams (SBR) latex and polybutadiene rubber (BR) latex were introduced initially as an extender for NR latex; later foam based entirely on such synthetic latices was developed. The most important commercial processes used for the manufacture of foam rubber even today are the Dunlop process and the Talalay process, even though the latter process accounts for less than 10% of the total foam rubber production.

9.2 Dunlop Process The Dunlop process can be run as a batch process or a continuous process. As in the case of every rubber product, a suitable formulation has to be selected in order to obtain a useful product. A typical formulation based on natural rubber latex is given in Table 9.1.

Table 9.1 Formulation 1: Natural rubber latex foam PART A (First stage compound) Compounding ingredients

Dry weight (g)

Wet weight (g)

Centrifuged natural rubber latex

100

167

Potassium oleate solution (20%)

0.5

2.5

Sulfur dispersion (50%)

2.0

4.0

ZDC dispersion (50%)

1.0

2.0

ZMBT dispersion (50%)

1.0

2.0

SP emulsion (50%)

1.0

2.0

Part B (Ingredients which are added to the compound during processing) Potassium oleate solution (20%)

0.5

2.5

Potassium castor oil soap solution (30%)

0.25

0.83

20

20

DPG dispersion (50%)

0.75

1.5

Zinc oxide dispersion (50%)

5.0

10.0

Ammonium acetate solution (20%)

1.0

5.0

Sodium silicofluoride dispersion (20%)

1.0

5.0

Colour concentrate dispersion (20%)

1.0

5.0

Kaolinite clay (dry powder)

208

Latex Foam Basically the formulation consists of four parts, namely, latex base, foaming agent, gelling agent and curing agent. Centrifuged natural rubber latex containing about 60% dry rubber content and ammonia as the preservative is the usual latex base used. Potassium oleate/caster oil soap is used as foaming agent. This also acts as a latex stabiliser when the ammonia content of the latex is reduced for foaming. Sodium silicofluoride is the primary gelling agent, while a zinc oxide/ammonium acetate combination acts as the secondary gelling agent. Diphenyl guanidine (DPG) acts as the foam stabiliser. A filler like kaolinite clay also may be used. Sulfur is the crosslinking agent while zinc diethyl dithiocarbonate (ZDC), zinc salt of mercaptobenzthiazole (ZMBT) are vulcanisation accelerators. Styrenated phenol (SP) is the antioxidant to protect the product against oxidative degradation. Colour may be added as required. The ammonia content of the latex has to be reduced before the foaming process. Usually compounding is done in two stages to obtain the optimal properties for the foam [6]. This is because it is advisable to mature the first stage compound for 24 hours to get uniform distribution of ingredients and partial precuring. The physical properties of the foam are also improved by the maturation of the initial compound.

9.2.1 Batch Process

9.2.1.1 Steps in the Batch Process The batch process involves the following operations: a) Preparation of dispersions, emulsions and aqueous solutions b) Deammoniation of latex c) Compounding d) Maturation e) Foaming (whipping) f) Refining (slow speed whipping) g) Addition of gelling agent h) Pouring the sensitised compound into the mould i) Gelling j) Curing k) Removal of the product from the mould l) Washing, drying and finishing 209

Handbook of Polymer Foams The various compounding ingredients are added as dispersions (in the case of water insoluble solids), emulsions (in the case of water insoluble liquids) and solutions (in the case of water soluble solids) [7]. The details of the steps are given in the next sections: a) Preparation of solutions, dispersions and emulsions • 20% potassium oleate soap solution Potassium oleate (20%) can be prepared by reacting potassium hydroxide and oleic acid in equimolar proportions with the required amount of water (part with oleic acid and part with potassium hydroxide) see Table 9.2.

Table 9.2 Formulation for potassium oleate soap solution Compound

Weight (g)

Oleic acid

100

Water

402

Potassium hydroxide

23.3

Water

43.0

A

B

A is warmed to 75 °C and then B is added to A using a high-speed stirrer. • 50% sulfur and accelerator dispersions The two dispersions are prepared as shown in Table 9.3.

Table 9.3 Formulations for sulfur and accelerator dispersions Sulfur mix Compound

Accelerator mix Weight(g)

Compound

Weight (g)

Sulfur

50

Accelerator

50

Dispersol F

1

Dispersol F

1

Soft Water

49

Soft water

49

210

formulation Potassium oleate soap solution formulations Sulfer formulations Accelerator dispersions

formulation for Antioxidant emulsion formulation for Filler slurry Latex Foam Both the mixes are ball milled for reducing the particle size and to form a stable dispersion. A dispersing agent, for example, Dispersol F (sodium methylene bis naphthalene sulfonic acid) is added to improve the stability by preventing chances of reagglomeration. Since sulfur is hard to disperse, the sulfur mix has to be ball milled for at least 48 hours while the accelerator mix needs only about 24 hours ball milling. • 50% antioxidant emulsion Water insoluble liquid antioxidant can be prepared as 50% emulsion in presence of ammonium oleate soap as stabiliser as shown in Table 9.4.

Table 9.4 Formulation for an antioxidant emulsion Compound

Weight (g)

Liquid antioxidant

100

Oleic acid

5

Ammonia (in water - 25%)

5

Distilled water

90

A

B

A is warmed to 75 °C and B is added to A with high-speed stirring. The emulsion is more stable due to the in situ formation of ammonium oleate soap. • 70% filler slurries Fillers like whiting, talc, lithopone, etc., can be added to latex to reduce the cost of the product. Excessive addition will affect the processing as well as the physical properties of the finished product. Filler addition improves hardness, which may be attractive for some applications. Normally they are added at a level of 25 to 30 parts per hundred parts of rubber (phr). Fillers can be added as aqueous slurries of about 70% solids content and can be prepared by the formulation given in Table 9.5.

Table 9.5 Formulation for filler slurry Compound

Weight (g)

Filler

10 0

Dispersing agent

2.0

Soft water

35-45

211

Handbook of Polymer Foams Normally ball milling is not required since the fillers are usually of low particle size. If the latex compound has good stability, fillers may also be added to latex directly as fine powder. b) Deammoniation of latex Normally, latex is preserved as either high ammonia (HA) latex concentrate (about 60% dry rubber content) or low ammonia (LA) latex concentrate. For HA latex concentrate (0.7% ammonia content), the ammonia content has to be reduced to 0.12 – 0.22%. This is usually done by blowing in a current of moist air over the surface of latex while it is being stirred by a drum shaped stirrer at about 50 rpm. Potassium soap may be added at a level of 0.25 to 0.5% to minimise any risk of destabilisation of the latex during deammoniation [8]. This amount of soap can however be deducted from the total amount of soap to be added to the mix. The deammoniation step can be avoided in the case of LA latex concentrate since its ammonia content is only 0.2%. c) Preparation of the compound Latex is mixed with the stabiliser and other ingredients as per the first stage compound formulation (Part A – Table 9.1). All water insoluble solid ingredients are added as dispersions and all water insoluble liquid ingredients are added as emulsions. The compounding ingredients are mixed with latex by gentle stirring. The ingredients added in the first stage (Part A) are soap (for the subsequent generation of froth), curing agent (sulfur and accelerator required for vulcanisation), an antioxidant (to inhibit ageing of the final product), and optionally mineral fillers. Mineral fillers of low particle size can be directly added to the latex as dry powders provided additional stabilisers are added to the latex or it can be added as slurry. Controlled addition of filler with proper stirring is essential to prevent destabilisation of the latex and locally concentrated layers. d) Maturation of the compound After the first stage compounding, the compound has to be matured for 24 hours. This is not done in the commercial process, but is known to improve the uniformity and quality of the product [9, 10]. e) Foaming (whipping) After maturation the compound is fed into a specially designed mixer known as a Hobart mixer. The Hobart mixer used for this purpose consists of a bowl in which a wire whip rotates in epicyclic (sun and planet) motion. The whip can have varying speeds. As whipping proceeds, the volume of foamed latex increases and passes through a maximum.

212

Latex Foam During whipping, the material in the vicinity of the whip gets processed whereas the larger part of the mix either lies dormant or is tumbled around the mixer in an otherwise inert fashion. Only a small amount of the compound is effectively processed at any time. The wire whip should move so fast that it can create a void behind it. The void gets filled with air and thus a large air bubble gets trapped in the latex compound. Subsequent rotation of the whip breaks the large bubble into little ones. This process is continued until the desired expansion is attained. The linear motion of the wire whip ensures the addition of more materials from the dormant zone to the processing zone. The last turn of the whip incorporates a few large air bubbles, which usually work to the surface of the compound and get discharged. So, at this stage the compound contains bubbles of varying range of sizes. f) Refining When the compound has attained the desired degree of expansion, the whipping speed is reduced and this process is called refining. During refining all the large air bubbles either get eliminated or comminuted, so that all the bubbles are of more or less uniform size. At this point the foam stabiliser is added. g) Addition of gelling agent Zinc oxide, ammonium acetate and a delayed action gelling agent – sodium silico fluoride (used for setting the foam before vulcanisation) are added separately in that order. As mentioned earlier the gelling agent is usually added as an aqueous dispersion (20% w/w) and its pH is adjusted to 6-7 just before addition to the latex compound [11]. h) Pouring the sensitised compound into mould The compound is immediately transferred into a two-piece mould (pre-warmed to 3040 °C) designed to produce the desired shape and size of the finished product. Mould shrinkage has to be taken into consideration when designing the mould. Slight excess material will overflow through the sides and the fine holes provided on the mould lid. This overflow is useful for checking the onset of gelling. i) Gelling Gelling is the destabilisation of the colloidal phase whereby the rubber particles join together to become a single entity. The gelling can be monitored by checking the consistency of the overflow material, which won’t come off easily once gelling has taken place. The gelling time depends on the amount of gelling agent used, and the temperature of the mould. Normally the time required for gelling is about 3-5 minutes.

213

Handbook of Polymer Foams j) Curing After proper gelling the mould is kept in a steam chamber for vulcanisation. The time of vulcanisation varies from 20-50 minutes depending upon the thickness of the final product. The majority of the commercial products like mattresses, cushions and pillows with thickness greater than 2.5 cm have a cored structure This structure is obtained by using moulds with regularly spaced pins/bushes which project (usually from the top plate of the mould) into the cavity of the mould, thereby giving a honeycomb structure to one side of the finished product. Earlier big bush moulds were used. They had bushes with a core size of 35-40 mm diameter and later the bush size was reduced to 18-22 mm for more uniformity. Nowadays pencil bush and pin core type moulds are used. For pin core moulds, the pins are made of aluminium rods having a diameter of 8-12 mm, whereas steel rods having a 6 mm diameter are used for pin core moulds. As the number of cores increases and their size decreases the rubber content of the mattress usually increases. However, in such cases the product may have a tendency to tear while being stripped from the mould, if it doesn’t have sufficient hot tear strength due to the decrease in wall thickness between cores. So, normally, only superior quality foam is made using pin core moulds. In pin core moulds, pins on both sides (lid and bottom of the mould) are preferred in order to make stripping easier. In such cases there is a middle layer of about 6-10 mm in between the cores. The mattresses made using pin core moulds need more time for drying, about 4-5 days whereas a small bush mattress needs only about 12-14 hours at 60-70 °C. Usually the drying of a pin core mattress is done in steps: drying for one day, then cooling, drying again for another day, and cooling, etc., for about 5 days. This process is more efficient in removing water from the inside of the foam rubber. k) Removal of the product from the mould After curing, the mould is taken out from the steam chamber and the wet cured product is stripped carefully from the mould. l) Washing and drying The product is washed in running water. This is done by passing it through a series of water sprays and squeeze rolls and finally through dry squeeze rolls to remove water. Washing removes residual water-soluble substances like soap, which can lead to poor ageing, poor resilience and bad odour. Finally, the foam is dried in an air-circulating oven kept at 60-70 °C for 12-14 hours in the case of a small bush mattress. The mattress made using pin core moulds needs more

214

Latex Foam time for drying, about 4-5 days and is usually done in steps: drying for one day, then cooling, drying again for another day and cooling, etc. During drying the product is laid flat without distortion to avoid permanent deformation. The products are usually laid on an open mesh grid. Products, if dried in contact with each other, have a tendency to stick together. Slight post curing takes place during drying. After drying, the products are trimmed to remove the flash and examined for defects. Defects such as tears and small surface problems can be repaired by using latex adhesive.

9.2.2 Selecting a Formulation for Latex Compounds • Latex Selection Natural rubber latex or synthetic latices like SBR latex, Neoprene latex or nitrile rubber latex can be used for making foam. Natural rubber latex is mainly used for commercial production. • Natural rubber latex Both high ammonia and low ammonia latex can be used for making latex foam. The two types should have the following specifications, for use in the manufacture of foam. Characteristics of high ammonia and low ammonia latex are given in Table 9.6.

Table 9.6 Characteristics of high ammonia and low ammonia latex High ammonia

Low ammonia

Total solid (%)

61.5

61.5

Dry rubber content (%)

60.0

60.0

Alkalinity (ammonia content of latex) (%)

0.7

0.2

Secondary preservative (%)

0.1

0.25

KOH number

0.45-0.65

0.45-0.95

Mechanical stability time (seconds)

600-1250

600-1200

Volatile fatty acid number

0.05-0.1

0.01-0.03

0.005-0.01

0.005-0.01

Coagulam content (%)

215

manufacture Latex foam Handbook of Polymer Foams Variation of total solid content and dry rubber content can lead to variable shrinkage resulting in variation in the size of foam products. The ammonia content of the latex is very important, as the gelling is pH dependent. The KOH number is the amount of potassium hydroxide needed to neutralise the total acid present in latex containing 100 g of dry rubber. This includes both volatile and non-volatile fatty acids, produced during the breakdown of the non-rubber constituents. The volatile fatty acid number represents the amount of KOH required to neutralise the volatile fatty acids in the latex sample containing 100 g total solids. The volatile fatty acids are mainly acetic acid, formic acid and propionic acid, which are formed from the breakdown of some of the non-rubber constituents present in the latex, when acted upon by bacteria. Mechanical stability time (MST) is an indication of the time period the latex can remain stable under high mechanical agitation, i.e., how effectively the rubber particles are protected in the latex [12, 13]. Two other important tests, which are recommended to be carried out, are the zinc oxide thickening test (ZOT), also called the zinc oxide viscosity test (ZOV), and the zinc stability time (ZST). ZOT and ZST represent the zinc sensitivity of the latex compound [14]. ZST is the change in MST of the latex mix with the addition of dry zinc oxide powder (5%), whereas ZOT is the change in viscosity of the latex mix with the addition of zinc oxide powder (5%) as a slurry. So ZST is directly proportional to the stability the latex mix while ZOT is inversely proportional to the stability. ZST and ZOT give a good indication of the foam rubber processability by the silicofluoride gelation in foam production. For good processability ZOV should be between 500-700. • Synthetic rubber latices The primary requirement for synthetic rubber latices is also that it should have good mechanical stability. The requirements are shown in Table 9.7.

Table 9.7 Requirements of synthetic rubber latices used for latex foam manufacture Property

Limit

MST (s)

1000

Dry Rubber Content (%) pH

50 10-11

The latices based on SBR and NBR usually contain carboxylated polymers. Carboxylated latices give foam rubber of higher wet gel strength. These latices are usually stabilised exclusively by fatty acid soaps. The styrene:butadiene ratio is in the range of 25:75. 216

Latex Foam Neoprene (polychloroprene) latex also can be used for the manufacture of foam rubber. The gel content should be low to facilitate particle integration and good wet gel strength. Sulfur modified polymer is used for foam rubber manufacture because of its higher wet gel strength and hot tear strength, which is necessary for foam as it is a cored product and has to be taken out from the mould at elevated temperature. Typical formulations based on nitrile rubber latex and Neoprene latex are given in Tables 9.8 and 9.9. Variation in dry rubber content may result in variation in shrinkage of the product and consequently products of low strength. Variation of ammonia content will result in variation in the gelling time. It is better to use latex aged for not less than 10 days and not more than 2 months.

9.2.3 Selection of Other Compounding Ingredients Foam promoters used in the Dunlop process are usually carboxylate soap, of which the most widely used are oleates, ricinoleates and castor oil soaps either alone or in combination. In general, mixtures of carboxylate soaps promote foaming more effectively than do the separate components. Castor oil soaps are less efficient as foam promoters compared to oleates, which are highly frothing and give fine froth. For natural rubber latex foam the amount of foam promoter required varies over a range of 0.5-2 phr. Synthetic latices normally

Table 9.8 Formulation for nitrile rubber latex foam Compound

Dry weight (g)

Wet weight (g)

Medium NBR latex (50%)

100

200

Sulfur dispersion (50%)

2.0

4.0

ZDC dispersion (50%)

1.0

2.0

ZMBT dispersion (50%)

1.0

2.0

Nonox SP emulsion (50%)

1.0

2.0

Zinc oxide dispersion (50%)

5.0

10.0

Ammonium acetate (20%)

1.0

5.0

Sodium silicofluoride (20%)

3.0

15.0

Part A

Part B

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polychloroprene rubber Latex foam

Handbook of Polymer Foams

Table 9.9 Formulation for polychloroprene rubber latex foam Compound

Dry weight (g)

Wet weight (g)

Sulfur modified polychloroprene latex (50%)

100

20 0

Zinc oxide dispersion (50%)

7.0

14. 0

Sulfur dispersion (50%)

1.0

2. 0

Thiocarbanilide dispersion (50%)

2.0

4. 0

2,2´methylene bis (4-methyl-6-tert butylphenol) dispersion (50%)

2.0

4. 0

ZDC dispersion (50%)

1. 0

2. 0

Sodium dibutyldithiocarbamate solution (25%)

1

4

O-dihydroxy benzene dispersion (50%)

1

2

0.1

0. 5

2

10

Part A

Part B

Foam stabiliser dispersion (20%) Sodium silico fluoride dispersion (20%)

require less foam promoter to get the same expansion, as they contain larger amounts of soap compared to NR latex. The foaming tendency is also dependent on pH. The pH range required for optimum foaming is 6-9. The ability to promote and stabilise foam depends on the hydrophobic moiety of the soap. Generally a longer hydrocarbon chain length improves efficiency but reduces its solubility in water [15, 16]. The vulcanising system used in the manufacture of latex foam rubber is sulfur in combination with accelerator and activator. The usual dosage used is sulfur (2 phr) and primary accelerator (1 phr) in combination with a secondary accelerator at a dosage of about 0.5 phr, and activator at about 1 phr. A commonly used primary accelerator is ZDC and as secondary accelerator ZMBT and zinc oxide as activator. The function of the secondary accelerator is to improve the elastic modulus of foam rubber and thus the load bearing capacity. Zinc oxide has the dual function of activator and gelling promoter. There are four classes of foam stabilisers used with the Dunlop process. 1. Quaternary ammonium surface-active compounds

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Latex Foam 2. Amino compounds 3. Organic hydroxyl compounds in particular phenols 4. Water-soluble hydrocolloids These are usually added in the second stage of compounding. They actually function as gel sensitisers rather than foam stabilisers. Commonly used quarternary ammonium compounds are n-hexadecyl trimethyl ammonium bromide, cetyl trimethyl ammonium bromide, etc. Amino compounds like DPG, triethylene tetramine, etc., are also used. The third class of compounds include nitrophenols, cresols, naphthols, etc. Principal examples of the fourth category of foam stabilisers, water-soluble hydrocolloids, are substances such as glue, casein, polyvinyl alcohol, etc. The amounts used are variable usually ranging from 0.1 to 0.2 phr. These materials enhance the stability of the aqueous phase/air interface by getting adsorbed at that interface and thereby the aqueous phase/rubber interface gets destabilised earlier compared to the aqueous phase/air interface, so that the latex gels before the foam has collapsed appreciably. So these materials can be described as gel sensitisers rather than foam stabilisers. Fillers are incorporated into latex foam rubber mainly to improve the stiffness of the product and to reduce cost. Filler addition also reduces shrinkage. As fillers are incorporated, the physical properties of the foam tend to deteriorate. Elongation at break and resistance to cyclic compression are reduced. At higher dosages of filler the product breaks down under cyclic deformation. Commonly used low cost fillers are talc, calcium carbonate, kaolinite clay, etc., up to 20-30 phr. Fillers can be added either as slurry or as fine powder, provided the latex is properly stabilised. Softeners such as mineral oil can be used at low dosages (up to 4 phr) to promote interparticle coalescence during gelation. Antioxidants like styrenated phenol or N,N´´di 2-naphthyl-p-phenylene diamine, etc., are used in latex foam rubber for improving the ageing resistance. Normally such antioxidants are used at a dosage of 1.0 to 1.5 phr. Addition of chlorinated paraffins, antimony trioxide, zinc borate and hydrated aluminium hydroxide, etc., can improve the flame resistance of latex foam rubber. Polychloroprene latex based foam rubber is found be flame resistant [17]. A commonly used gelling agent is sodium silicofluoride in combination with zinc oxide. The sodium salt is preferred in natural rubber latex whereas a combination of sodium and potassium salt is used in synthetic latices. In NR latex about 1.5 phr of sodium silicofluoride is used together with about 3-5 phr of zinc oxide. The gelling is found to be highly influenced by the pH, the optimum value being approximately 8.6. Gelling can be retarded by addition of a solution of dilute aqueous alkali to the silicofluoride dispersion [18]. Commonly used alkalis are ammonium hydroxide, sodium hydroxide and trisodium

219

Handbook of Polymer Foams orthophosphate. Normal practice is to adjust the pH of sodium silicofluoride to at least 7 and then add to the foamed latex. Gelling in the Dunlop process involves the following steps. The latex compound contains ammonia and soap in addition to the curing ingredients. After frothing, zinc oxide and sodium silicofluoride are added separately. The pH of the mix is in the range of 10.010.5. At this pH sodium silicofluoride hydrolyses slowly as shown [19]: Na2SiF6 → 2Na+ + SiF6 2SiF6 2- + 4H2O → Si (OH) 4 +4H+ + 6FThe hydrolysis brings about gelation of the latex foam in three ways: 1. The fall in pH due to the presence of hydrofluoric acid. 2. The absorptive effect of silicic acid 3. The destabilisation effect of zinc amine complex formed by the reaction of zinc oxide with ammonium fluoride, which is formed by the reaction between hydrofluoric acid (HF) and ammonium hydroxide (NH4OH). These zinc amines when destabilised attack soaps in latex to form insoluble zinc soap. By adjusting the levels of zinc oxide and sodium silicoflouride and by the use of secondary gelling agents such as diphenyl guanidine, cetyl trimethyl ammonium bromide, etc., the reactions leading to the destabilisation of the air liquid system and the rubber liquid system can be balanced to get an open cell foam. The foamed latex is essentially a three-phase colloidal system. It comprises of two dispersed phases, rubber particles and the air bubbles and a single continuous water phase. Of course there are other dispersed phases such as fillers, curing agents antioxidants, etc. These dispersed phases are of comparatively minor importance for the fundamental processing technology of foamed latex and for the behaviour of the foamed latex colloidal system. There exist two interfaces, one between the latex aqueous phase and rubber particles and the second between aqueous phase and air bubbles. The successful manufacture of foam rubber depends on the proper manipulation of these interfaces. As the same stabilisers give stability to both interfaces the destabilisation of one interface always results in the destabilisation of the other interface. However, for the production of foam, the destabilisation of the water/rubber interface should occur first and then only the destabilisation of water/air interface should occur. If the destabilisation of the water/air interface occurs first, the foam will collapse. To avoid this, the foam stabiliser should preferentially stabilise the water/air interface. Pure latex foam is off white in colour. Depending upon the requirement, colour may be added. Photographs of the process are shown in Figure 9.1. 220

Latex Foam

Figures 9.1a-p Foam compounding process

Figure 9.1a Deammoniation process

Figure 9.1b Measuring the latex for compounding

221

Handbook of Polymer Foams

Figure 9.1c Compounded latex in the mixer for foaming (whipping)

Figure 9.1d Open mould

222

Latex Foam

Figure 9.1e Pouring foamed latex into the mould from the mixer

Figure 9.1f Spreading the foamed latex compound in the mould

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Handbook of Polymer Foams

Figure 9.1g Closed mould in the steam chamber

Figure 9.1h Mould opening after curing

224

Latex Foam

Figure 9.1i Product stripping

Figure 9.1j Washing the product in water

225

Handbook of Polymer Foams

Figure 9.1k Passing through rollers

Figure 9.1l Final pass through squeeze rollers

226

Latex Foam

Figure 9.1m Laying the product on wire net for oven drying

Figure 9.1n Samples in the drier

227

Handbook of Polymer Foams

Figure 9.1o Trimming of the product

Figure 9.1p Foam mattress

228

Latex Foam

9.2.4 Continuous Process for Latex Foam Production Modern high capacity latex foam plants use continuous foaming process. The motivation for the continuous process is two fold: to reduce labour cost and to reduce compound variation thereby improving product uniformity. A typical example is the production of latex foam rubber using an Oaks mixer. The Oaks mixer used in this process is similar to the Hobart mixer in the batch process but which is designed to mix continuously. The first continuous latex foaming process was patented by Murphy and co-workers [20]. Compounded latex and air are metered into the base of a long vertical chamber and beaten to foam. The foamed latex compound is fed into another chamber, which is also provided with a beater, where dispersions of zinc oxide and gelling agent are added and then it is fed into the mould. After gelling it is cured. The advantages for the products made by the continuous process are: a) they are more uniform and have a superior texture b) variation of foam density is possible c) reduction in whipping time compared to batch process for getting the same density foam d) material wastage in the bowl can be reduced e) rejection rate can be reduced f) labour cost is reduced The mixer head is constructed with stainless steel and can be easily dismantled and cleaned. The head consists of a rotor, which is completely enclosed with two stators. The rotor has a large number of square section teeth arranged in concentric circles. The stators also have teeth arranged similarly, spaced in between the teeth on the rotor as shown in Figure 9.2. The latex compound is fed into the mixer along with required amount of air by way of the inlet shown. The compound enters the mixing chamber, which is formed, between the rotor and the stator. As the rotor rotates it intimately mixes the material in between the teeth of the rotor and the stator. The mixing achieved may be described as being twodimensional: the material moves in a tangential direction; as the rotor revolves it also moves radially from one circular path to another under the influence of the incoming material. So all the material gets processed to the same extent. As the latex compound and air get mixed, it results in fine-celled foam of uniform structure. It is claimed that natural rubber latex foam of specific gravity as low as 0.06 can be made by this method. Such a low density needs the latex compound to have about 17 times expansion. The ratio of air to latex can be varied to make latex foam rubber of varying density. The rotor speed is

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Handbook of Polymer Foams always kept as low as possible, usually in between 100 and 400 rpm. Zinc oxide and sodium silicofluoride are injected into the mix using a hypodermic syringe. A typical layout of the continuous process is shown in Figure 9.3.

Figure 9.2

Figure 9.3 Lay out for the continuous Dunlop process

230

Latex Foam Steps in the process are: a)

Cleaning of the mould

b)

Application of a mould release spray

c)

Drying of the mould

d)

Inspection of the mould

e)

Warming of the mould

f)

Opening of the mould

g)

Filling of the mould with latex foam

h)

Closing of the mould

i)

Gelation of foam

j)

Vulcanisation of the foam

k)

Cooling of the mould

l)

Opening of mould

m) Stripping of the product

9.3 Talalay Process The Talalay process is different from the Dunlop process in that the chemical gelling agent in the latter process for setting the foam is replaced by carbon dioxide in the former and hence is more environmentally friendly. However, as in the Dunlop process this also requires accurate control in which rubber/water and water/air interfaces collapse and are manipulated by the matrix temperature [21]. Dr. Anselm Talalay of BFGoodrich Sponge Products is the pioneer of the Talalay process. There have been minor changes in the process over the years and the modern Talalay process can be divided into the following operations: a) Preparation of dispersions, emulsions and solutions b) Deammonisation in the case of natural rubber latex c) Compounding d) Maturation

231

Handbook of Polymer Foams e) Foaming f) Pouring the foamed compound into the mould and vacuum expansion g) Freezing h) Gelling i) Curing j) Removal of the product from the mould k) Washing, drying and finishing The compound preparation is similar to that for the Dunlop process. Usually the Talalay process uses SBR latex or a blend of SBR and NR latex, probably because the process is more popular outside the NR producing countries in the world. It may be observed that the basic process used is more or less the same as that of the Dunlop process except the gelling stage. Silicafluoride gelling agent is avoided in this process. Since the latex base is likely to be ammonia free, a small amount of ammonia is added to improve the gelling. KOH and Vulcastab VL (polyethylene oxide condensate) are added as the stabilisers. A small amount of process oil is added to improve the flexibility of the product. Sulfur along with accelerator and zinc oxide function as the curing system while Nonox SP is used as the antioxidant. The Talalay process is generally not used for the manufacture of speciality foams based on nitrile or Neoprene latex. A typical formulation using SBR latex is given in Table 9.10. In one process the expansion is brought about by the chemical decomposition of hydrogen peroxide by an enzyme. The latex compound after maturation is mixed with the required amount of hydrogen peroxide and a slurry of bakers yeast preferably at a low temperature (about 10 °C) to delay the decomposition of the peroxide. The mixture is then quickly placed in a specially designed mould (Figure 9.4). The enzyme catalase (EC 1.11.1.6) present in the yeast decomposes hydrogen peroxide to liberate oxygen, which expands the compound into a froth. Due to the difficulty in controlling chemical frothing, in the modern process this is replaced by a combination of mechanical frothing and vacuum expansion. Gelling agents are not used. The partially expanded froth is placed in the mould and as the mould is closed vacuum is applied so that the froth expands and fills the mould. Products of varying density can be made by this method by adjusting the froth density in the mixer. Due to the complicated design of the mould it is difficult to apply a mould-releasing agent in the Talalay mould. This is overcome by the use of an internal lubricant added to the froth prior to it entering the mould. The usual lubricant is a small amount of dilute hydrogen peroxide solution, which is blended with froth just prior to feeding it in to the mould.

232

formulation SBR latex Latex Foam

Table 9.10 A typical formulation using SBR latex Dry weight (g)

Wet weight (g)

SBR latex (50%)

100

20 0

Polystyrene co-agglomerated with SBR latex (50%)

17.5

35

Potassium oleate solution (20%)

0.5

2. 5

Process oil emulsion (40%)

2. 0

5. 0

Nonox SP emulsion (50%)

1.0

2. 0

Sulfur dispersion (50%)

1.5

3. 0

Vulcastab VL solution (20%)

0.25

1.2 5

Zinc oxide dispersion (50%)

5.0

10. 0

ZDC dispersion (50%)

1.25

2. 5

ZMB dispersion (50%)

0.6

1. 2

Ammonia solution (35%)

2.0

6. 0

Potassium hydroxide solution (10%)

0.1

1. 0

Figure 9.4 Cross sectional view of typical Talalay mould

233

Handbook of Polymer Foams The gelling and curing are controlled by heating, cooling process and so the mould should have provisions for effective heating and cooling rapidly and reliably. The mould is fitted with channels through which glycol/water mixture at precisely controlled temperature are circulated, and the heat is conducted into and out of the foam by a series of closely spaced pins penetrating the foam from both surfaces of the mould. Four glycol/water streams are used to get the following temperatures: Cold

30 °C

Low intermediate –4 °C High intermediate –38 °C Hot

110 °C

The mould periphery is fitted with a double groove with a vacuum moat between the two grooves. The outer groove is provided with a permanent temperature resistant rubber gasket, which seals the mould cavity with an air tight fit when the mould is closed. The inner groove is fitted with a replaceable semi permeable paper gasket through which air or gas can pass but froth cannot pass. When the required amount of the partially foamed compound is metered into the mould, the mould closes and vacuum is applied to the moat which withdraws the air from the mould, through the paper gasket. This causes the foam to expand and fill the mould cavity. An automatic valve then operates to circulate glycol/water mixture at –30 °C through the passage in the mould causing the expanded foam to freeze rapidly. The rapid rise in surface tension destabilises the air/water system and this together with the growth of ice crystals, causes the air bubbles to connect together resulting in the formation of open cell foam. There is a chance for the collapse of the foam during destabilisation of the air/water interphase but this is prevented as the froth is in the frozen state. With cold glycol/water mixture still circulating vacuum is removed and carbon dioxide is pumped into the moat. Here it passes through the paper and the frozen foam. The pH falls from about 12 to 9.5 and the rubber-water phase breaks down due to precipitation of zinc soaps from the destabilisation of zinc amines, and the formation of zinc carbonate. When the rubber is coagulated in a stable foam structure, the mould and its contents are rewarmed with the so-called intermediate glycol/water mixture. The high intermediate and finally hot glycol/water mixture is passed through the mould. The final stream raises the temperature to 110 °C and the foam is kept at this temperature for curing. The time schedule of the various processes is given in Table 9.11. At the cure temperature, as ammonium carbonate breaks down into ammonia and carbon dioxide, the pH rises and it causes the reformation of potassium oleate soap, which aids the removal of the foam from the mould. Further, as the lid of the mould is hotter than the base, the product gets withdrawn from the pins in the base and is held on to the pins in the lid, where it is easier to strip. In order to get high contact area and to have efficient heat transfer a number of closely spaced pins are provided in the mould. The compound

234

Latex Foam should be designed to have high hot wet tear strength to avoid damage during stripping of the product from the mould. Finally the product is washed and dried. Typical Talalay foams are shown in Figure 9.4.

Table 9.11 Time schedule for various operations Time (min) Vacuum expansion

2

Freezing (cold)

8

Carbon dioxide gassing

5

Low intermediate

2

High intermediate

2

Hot (cure)

10

Drying (post cure)

7.5

Figure 9.4 Examples of Talalay foams

9.4 Troubleshooting in Latex Foam Manufacture Since foam manufacture involves the interplay of the stability of different interfaces, the quality of the product will be affected if the process isn’t properly controlled. The commonly observed defects in latex foam are given in Table 9.12.

9.5 Testing The testing of latex foam is generally done as per ASTM D1055-97 [22]. Latex grades have their grade numbers designated by two letters which identify the kind of latex foam rubber as follows: 235

Handbook of Polymer Foams

Table 9.12 Common defects observed and their remedies Nature of defect

Possible Reason

Remedy

1

Coarse structure and Gelation at too low a pH rat holes

Increase the dosage of secondary gelling agent

2

Loose skin

Slow gelling due to either insufficient gelling agent or mould too cold

Increase dosage of gelling agent and/or use a warmer mould

3

Thick skin

Mould too hot

Use cooler mould

4

Flow marks on the surface

Mould too hot or gelation too fast

Use cooler mould and/or reduce gelling agent

5

Surface lakes

Excess mould release agent

Reduce the amount of mould release agent

6

Splitting in the centre

Gelation too fast

Reduce the dosage of gelling agent and/or use cooler mould

RC – Latex foam rubber, cored and RU – Latex foam rubber, uncored

9.5.1 Compression Set Compression set under constant deflection is measured using a cylindrical test specimen having 29 mm height and diameter not less than 19 mm. The apparatus and procedure are described in method B of ASTM D395 [23]. Here the sample is compressed to 50% of its original thickness in between two aluminium plates and the sample is kept at 70 °C for a specified time. The force is released at the end of the test and then the thickness of the sample after 30 minutes at room temperature is measured. The constant deflection compression set can be expressed either as a percentage of the original height or as a percentage of the original deflection as shown in the following equations: Compression set in original height

Ch =

t 0 − t1 x100 t0

Compression set in original deflection

Cd =

t 0 − t1 x100 t0 − t s

where:

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Latex Foam to = original height of test specimen t1 = height after removal from the apparatus ts = height of the spacer bar The compression set of the sample should not exceed 15%

9.5.2 Indentation Hardness A flat circular indenter foot 0.03 m2 in area is connected to a force measuring device by means of a ball and socket joint, and mounted in such a manner that the specimen can be deflected at a rate of 0.2 to 10 mm/s. A maximum radius of 2 mm is allowable on the edge of the indentor foot. The sample is supported on a perforated horizontal plate to allow rapid escape of air during the test. The test specimen should have at least 300 mm x 300 mm surface for indentation and a thickness of not less than 19 mm. The test specimen is placed on the perforated plate in such a way that the cored or honeycombed surface faces the perforated plate. The specimen position should be such that the indentation is made at the centre. The indenter foot should be brought into contact with the specimen and the original height determined after applying an initial force 4.5 N, then compressing the specimen to 25% of the original height and observing the load in Newtons including the 4.5 N preload. This is usually measured at 23 ± 1 ºC and 5.0 ± 2% relative humidity after conditioning the sample for 12 hours. The indentation hardness index is the load in kilograms required to give an indentation in the sample equal to 40% of the original thickness under specified conditions. It is a measure of the load bearing capacity of the foam. Foam products are graded as A B C D E F G and H according to their indentation hardness index as shown in Table 9.13. The hardness change of the sample after ageing at 70 ± 1 oC for 168 hours should be within ± 20%.

9.5.3 Flexing Resistance The flexing test consists of subjecting the sample to repeated compression and noting the effect on cellular structure. The amplitude of compression and decompression should vary between 25% and 50% of the thickness of the sample depending upon the indentation value. Failure of the specimen is evidenced by the break down of the cellular structure as observed by visual examination.

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indentation hardness Latex foam Handbook of Polymer Foams

Table 9.13 Indentation hardness grading of latex foam Grade

Indentation hardness index

A

7–14

B

15–21

C

22–28

D

29–34

E

35–45

F

46–55

G

56–65

H

66–75

9.5.4 Density The density of foam rubber is a measure of the expansion which is calculated by taking the weight in air and loss of weight in water. A sinker has to be used to sink the foam sample in water. The surface of the test piece must be coated with wax to prevent water absorption when immersed in water. The measurement is done at a temperature of 20 °C.

9.5.5 Metallic Impurities Maximum amount of copper and manganese in the foam should be copper (0.001%, by weight) and manganese (0.005%, by weight). The product should not have any objectionable odour. The colour should be as per the specifications.

9.6 Important Uses of Latex Foam

9.6.1 Transportation Transportation is the single largest outlet for latex foam. Depending upon the specific need, products of different properties are needed. Automobile seating has a variety of 238

Latex Foam shapes and designs. This may vary from a foam pad resting on a spring or full depth cushioning in the case of a light motor vehicle. The back support in automobile seating has to resist only a minor load and consequently can be made of a much lighter density foam. In the case of bus seating a high density shallow seat may be good enough due to the frequent interchange of passengers. For a coach, the seat design must obviously be more luxurious. An aircraft seat does not need to absorb much vibrations. It should have sufficient padding to accept body contours and remove high pressure contact areas for comfort. For train seats also, there is not much need for vibration absorption. Mainly it is the static seating comfort which is of significance. Motor cycle seats generally require a foam of very high density, partly because of the intensity of the shock that has to be absorbed and partly because of the high loading per unit area.

9.6.2 Furniture The static requirements of foam rubber cushioning, for example mattresses, are different from the dynamic ones in transport. The main objectives in this case are the optimum support of the body and comfort. The cavity pattern of the mattress and the movement of air through the surface due to the highly porous nature of the product and the pumping action on deflection, etc., add to comfort. In hospital and institutions the foam rubber mattress is of particular advantage due to the simplicity of bed making, and its nondusting and bactericidal attributes. The pillow uses one of the lowest density products.

9.6.3 Special Uses In addition to the conventional uses mentioned above, there are other special uses such as therapeutic cushions, packing material for electronic equipment and household goods, gap fillers, shock absorption, shoe insoles, lining for many products, etc.

References 1.

F.H. Untiedt, inventor; no assignee; US1777,945, 1930.

2.

E.A Murphy, W.H. Chapman and D.W. Pounder, inventors; Dunlop Rubber Company Ltd., assignee; GB332, 525, 1930.

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Handbook of Polymer Foams 3.

E.A. Murphy, Transactions of the Institution of the Rubber Industry, 1955, 31, 90.

4.

E.W. Madge, Latex Foam Rubber, Maclaren and Sons, London, UK, 1962.

5.

J.A. Talalay, inventor; no assignee: GB 455,138, 1938.

6.

D.C. Blackley, Polymer Latices - Science and Technology, Volume 1: Fundamental Principles, 2nd Edition, Chapman and Hall, London, UK, 1997.

7.

R.L. Kelly, Proceedings of the 123rd ACS Rubber Division Meeting, Toronto, Canada, Spring 1983, Paper No.12.

8.

C.W. Jurado and K.G. Mayhan, Rubber Chemistry and Technology, 1986, 59, 1, 84.

9.

M.E. Myers Jr., A.M. Wims and W.R. Lee, Rubber Chemistry and Technology, 1973, 46, 2, 464.

10. E.B. Bradford and J.W. Vanderhoff, Rubber Chemistry and Technology, 1968, 41, 2, 514. 11

B.J. Newey and R.G. James, inventors; International Latex Process Ltd., assignee; GB 574, 131, 1945.

12. A.D.T. Gorton, Rubber Chemistry and Technology, 1972, 45, 5, 1202. 13. H.C. Chin, M.M. Singh and S.C. Loke, Plastics and Rubber: Materials and Applications, 1979, 4, 164. 14. D.C. Blackley, Polymer Latices - Science and Technology, Volume 3: Applications of Latices, 2nd Edition, Kluwer Academic Publishers, Dordrech, The Netherlands, 1997. 15. G.D Miles and Ross, Journal of Physical Chemistry 1944, 48, 280. 16. A.D.T. Gorton, Rubber Chemistry and Technology, 1970, 43, 5, 1255. 17. C. Anolick, G.S. Cook and C.W. Stewart, Rubber Chemistry and Technology, 1979, 52, 4, 871. 18. H.E. Schweller, Proceedings of the 123rd ACS Rubber Division Meeting, New Orleans, LA, USA, Fall 1975, Paper No.5. 19. J.C. Fallois in Polymer Latices and their Applications, Ed., K.O. Calvert, Applied Science Publishers, London, UK, 1982, 207-228.

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Latex Foam 20. E.A. Murphy, Transactions of the Institution of Rubber Industry, 1955, 31, 90. 21. E.V. Thomas in Rubber Products Manufacturing Technology, Eds., A.K. Bhowmick, M.M. Hall and H.A. Benarey, Marcel Dekker, New York, NY, USA, 1994, 845-853. 22. ASTM D1055-97, Standard Specifications for Flexible Cellular Materials-Latex Foam, 1997. 23. ASTM D395-02, Standard Test Methods for Rubber Property—Compression Set, 2002.

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Microcellular Foams

10

Microcellular Foams Vipin Kumar and Krishna V. Nadella

10.1 Introduction Microcellular foams refer to thermoplastic foams with cells of the order of 10 μm in size. Typically these foams are rigid, closed-cell structures, although recently there is much interest in creating open-cell, porous structures that have cells in this size range. The microcellular process that sparked the growth in this field over the past two decades was invented at Massachusetts Institute of Technology, USA, in the early eighties [1], in response to a challenge by food and film packaging companies to reduce the amount of polymer used in their industries. As most of these applications used solid, thin-walled plastics, reducing their densities by traditional foaming processes that produced bubbles larger than 0.25 mm was not feasible due to excessive loss of strength. Thus was born the idea to create microcellular foam, where we could have, for example, 100 bubbles across 1 mm thickness, and expect to have a reasonable strength for the intended applications. It would be reasonable to say that the potential of microcellular foams has yet to be realised. These materials have not yet appeared in mass produced plastic items, and the promised savings in materials and associated costs have yet to materialise. This is largely due to manufacturing difficulties encountered in scaling up for large scale production. However, enthusiasm for these materials remains high, and today researchers and commercial enterprises on every continent are in a global race to harness the potential benefits. Much has been learned about the processing and properties of microcellular foams since the first patent was granted in 1984 [2]. An early review of the subject appeared in 1993 [3]. In this chapter the state-of-the art of processing will be reviewed in the next section, followed by a discussion of structure and properties. This chapter will conclude with a look at some of the current research directions involving microcellular technology.

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10.2 Processing of Microcellular Foams

10.2.1 The Solid-State Batch Process The basic solid-state microcellular process is a two-stage batch process shown schematically in Figure 10.1. In the first stage, the polymer is placed in a pressure vessel with a high-pressure and a non-reacting gas. This step is usually conducted at room temperature. Over time, the gas diffuses into the polymer, and attains a uniform concentration throughout the polymer specimen. When this specimen is removed from the pressure vessel and brought to atmospheric pressure, a ‘supersaturated’ specimen

Sample Foamed sample

CO2 gas cylinder

Pressure vessel

Heated bath

Stage I Saturation of specimen

Stage II Foaming of specimen

Figure 10.1 Schematic of the batch process to make solid-state microcellular foams

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Microcellular Foams that is thermodynamically unstable due to the excessive gas dissolved into the polymer is produced. In the second stage, the supersaturated specimen is heated to a temperature above the glass transition temperature (Tg) of the polymer-gas mixture, termed the foaming temperature. This step is typically carried out in a heated bath with temperature control. The dissolved gas lowers the Tg of the polymer [4] and the foaming temperature needs only to be above the Tg of the gas-polymer system in order for the bubbles to nucleate and grow. Since the polymer is still in a solid state, the foams produced are called ‘solid-state foams’ to distinguish them from conventional foams that are typically produced in an extruder from a polymer melt. The term ‘solid-state’ is meant to convey an essential difference from the extrusion processes, namely that in the former process the bubbles are formed in the rubbery state, near the Tg and the polymer is never melted. Thus, while surface tension effects play an important role in the bubble growth dynamics of extrusion foams, these effects are not important in the solid-state process. Instead, the viscoelastic properties of the gas-polymer system become important. The solid-state batch process has been used to create microcellular foams from a number of amorphous and semi-crystalline polymers, such as polystyrene (PS) [1, 5-7], polycarbonate (PC) [8, 9], acrylonitrile-butadiene-styrene (ABS) [10], polyethylene terephthalate (PET) [11], glycol-modified PET (PETG) [12], crystallisable polyethylene terephthalate (CPET) [13], and polyvinyl chloride (PVC) [14], etc. Examples of solidstate microcellular structures in several polymers are shown in Figure 10.2. The microcellular structure is remarkably uniform compared to the structure in extruded foams or structural foams. A unique aspect of the batch process is the ability to create an integral unfoamed skin on a foam specimen [15]. This can be understood with reference to Figure 10.3, which shows gas concentration profiles in a saturated specimen, just after it is removed from the pressure vessel (time zero) and at a later time t. During this time, called desorption time, the gas is allowed to escape from the surface layers. Then if C* is the minimum gas concentration needed for bubble nucleation, one can see that there is a surface layer in which bubbles will not nucleate due to a lack of sufficient amount of dissolved gas. Thus a skin of solid polymer with a desired thickness can be created when the specimen is heated after a suitable desorption time. This provides a means to create skin-core structures that can be optimised to achieve the desired properties. The basic solid-state microcellular process discussed above is called a temperature soak process to signify that after initial saturation of the polymer by gas, bubble nucleation is induced by heating the polymer. The reduction in gas solubility upon heating provides the driving force for bubble nucleation. The bubble nucleation can also be achieved by a

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Figure 10.2 Examples of microcellular foams in a number of thermoplastics: (a) PVC; (b) PC; (c) ABS; (d) PET. All specimens show a remarkable homogeneity in microstructure. The cell sizes range between 1-10 μm except for PET where the cells are in the 100 μm range

sudden reduction of pressure, provided that the gas-saturated specimen is already above the glass transition of the polymer-gas system. This is called the pressure-quench method, and has been used for creating microcellular foams using supercritical carbon dioxide [16-18]. This method has also been used to create open-cell microcellular foams discussed later in Section 10.4.2. Bubble nucleation in the solid state process was first studied by Colton [5] who applied classical nucleation theories to this process. Later experiments by Kumar [6] and Kweeder and co-workers [7] showed that classical theories did not adequately explain nucleation in the solid state. This is the subject of on going inquiry.

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Figure 10.3 Schematic showing the creation of an integral, unfoamed skin in the batch microcellular process

10.2.2 The Semi-Continuous Process A process to scale-up the batch process in order to produce a roll of microcellular sheet was proposed by Kumar and Schirmer [19, 20] and is shown schematically in Figure 10.4. Normally, if a roll of polymer film of say 10 cm radius was put in the pressure vessel for saturation with gas, it would take hundreds of years at the typical rates of diffusion for the gas to achieve a uniform concentration throughout the polymer roll. The breakthrough idea in the semi-continuous process is that the polymer roll is first interleaved with some sort of gas channelling device, such as a roll of paper towel. When this roll is now put in the pressure vessel, the entire roll gets saturated in the same amount of time that it takes for one polymer layer, which is of the order of hours to days depending on the gas and polymer under consideration and the thickness of the polymer sheet. As shown in

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Figure 10.4 Schematic of the semi-continuous process for industrial scale production of solid-state microcellular foam sheets. Paper towel was used in the laboratory to establish feasibility of the process

Figure 10.4, the gas-saturated roll is passed through a hot bath to create the foam, and a chilled bath to quench the microstructure, and the foamed polymer roll is collected as shown. The gas-channelling device (paper towel in the laboratory version of the process) can be collected and re-used. A laboratory-scale machine was built by Branch [21] to investigate the key processing parameters of the semi-continuous process. In this design a breaking mechanism was incorporated in order to systematically vary the tension in the line. The effect of tension on the structure and properties of the microcellular foam was investigated. It was found that the tension in the line does not affect the density of the foams. However, the tension elongates the cells in the processing direction. One consequence of this alignment in the tension direction is that the tensile strength in the semi-continuous specimens is about 10% higher at a given relative density, compared to the foams produced by the batch process.

10.2.3 Extrusion and other Processing Methods Since the first patent on a process to make microcellular foams was issued [2], a number of efforts have been made to enable large-scale production of these novel materials. The

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Microcellular Foams strongest emphasis has been on development of extrusion processes (see, for example, Park and co-workers [22, 23], Shimbo and co-workers [24], and Seibig and co-workers [25]). Other developments include a thermoforming process (Kumar and Suh [26]), and a sintering process where gas-saturated powder is first compacted and then heated to create a net-shaped part (Seeler and co-workers [27, 28]). A semi-continuous process to convert a roll of film to a roll of solid-state microcellular foam as described previously presents an alternative to extrusion for production of foam sheets. Technology for producing microcellular parts in injection moulding has been developed at Trexel [29]. As the interest in this technology grows and we get closer to commercial realisation, an understanding of the development of microstructure in these processes becomes important both from the viewpoint of process control as well as for optimisation of the properties of the final product. For the extrusion-based processes, where the bubbles are formed in a polymer melt, a number of studies have been made that address the issues related to the growth of bubbles (see for example, Gent [30], Saunders [31], Arefmanesh [32, 33], and Ramesh [34]). This subject has been reviewed by Ramesh [35] where one can find the related bibliography. Carbon dioxide is by far the most widely used gas for solid-state microcellular processing [8-14, 18, 36]. Microcellular foams have also been produced by a polymer solvent phase separation process [37, 38]. Recently Handa and Zhang [39] have presented a novel stress induced nucleation process to obtain a variety of microcellular structures.

10.3 Properties of Microcellular Foams Although innovations in processing have developed at a rapid pace, the property data on microcellular foams have been slow in coming. The early publications on microcellular foams conjectured that the microcellular structure, believed to be on a scale that was smaller than the ‘critical flaw size’ for polymers, would enable these foams to retain their mechanical properties even as the density was reduced. No quantitative information on the critical flaw size was ever presented, nor was any property data presented in support of the hypothesis. This is likely to be due to the emphasis placed on process development, as opposed to property characterisation, in the early years of evolution of this field. Over time, however, this conjecture has become a myth that microcellular materials are as strong as the solid polymers but have a lower density, thus providing an opportunity to lower costs with no penalty in performance. The tensile property data [40] show that the tensile strength of microcellular foams decreases in proportion to the foam density, and can be approximated quite well by the rule of mixtures. Thus a 50% relative density foam can be expected to have 50% of the strength

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Handbook of Polymer Foams of the solid polymer. Figure 10.5 shows relative tensile strength as a function of relative foam density for a number of microcellular polymers. In this figure the relative tensile strength, is obtained by dividing the tensile strength of the foam by the tensile strength of the solid polymer. Similarly, the relative density is foam density divided by the solid polymer density. In Figure 10.6 we have plotted the strength data on a specific basis. Thus the specific relative tensile strength for the foam of a given relative density is obtained by dividing the relative tensile strength by the relative density. Figure 10.6 shows that on a specific basis, the tensile strength of microcellular foams is essentially constant over the entire range of foam densities. Unfortunately, similar data on conventional foams is not readily available for a direct comparison with microcellular foams. A unique aspect of data in Figure 10.5 is that in the relative density range of 0.1 to 0.5, the microcellular foams represent novel materials for the engineer with properties not previously available. Most conventional foams fall either in the low-density region (relative density less than 0.1) or belong in the structural foams category (relative density greater than 0.5). The modulus of microcellular foams can be reasonably estimated by the GibsonAshby cubic cell model [41], which predicts that the relative tensile modulus equals the square of the relative density. The gas composition in the cell may affect the long term thermal conductivity of the foams [42]. Microstructures, tensile strength, and thermal

Figure 10.5 Tensile strength data on microcellular foams produced by the batch process. The tensile strength is closely approximated by the rule of mixtures over the entire range of foam densities

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Figure 10.6 Plot of specific relative tensile strength as a function of relative density of microcellular foams. Note that specific strength is essentially constant over a wide range of foam densities

expansion properties for a number of low density foams have been reviewed by Williams and Wrobleski [43]. Fatigue and creep behaviours of microcellular polycarbonate foams have been investigated [44-46]. An interesting result from fatigue studies is that introduction of very small bubbles in PC, with less than 1% reduction of density, led to a thirty-fold increase in fatigue life compared to the solid PC. This might suggest a process similar to heat treatment of metals, where a PC part may be saturated with carbon dioxide at 5 MPa and then heated to say 60 ºC to introduce the microcellular structure without an appreciable density change, to increase the fatigue life of a part. Due to the low processing temperatures, very little dimensional change was observed in the experiments. The tensile data for all gas-polymer systems investigated falls on one reduced plot where relative tensile strength can be plotted against the relative density, as is shown in Figure 10.5. However, energy absorption measures, such as an impact test, are more sensitive to variations from polymer to polymer, and the results cannot be generalised. Figure 10.7 shows Gardner impact strength for PVC foams [47] with relative densities of

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Figure 10.7 Gardner impact strength of microcellular PVC foams as a function of foam relative density. The impact strength is seen to be independent of the saturation pressure used to prepare the foam specimens [47]

0.5 and higher. It is seen that the impact strength decreases linearly with foam density. This result is contrary to the popular belief, long held without proof, that the microcellular structure will always improve the energy absorption behaviour due to the increased resistance to crack propagation offered by the micro voids [48]. Another point to note from Figure 10.7 is that the gas saturation pressure used to prepare the foam specimens appears to have no significant effect on the impact resistance. Such is not the case for the impact resistance of CPET foams [13], shown in Figure 10.8. We find that foams prepared at 5 MPa carbon dioxide pressure have significantly higher impact strength than the foams prepared at 3 or 4 MPa pressure. In this system, there is crystallisation of CPET at 5 MPa, that changes the composition of foam matrix, and results in entirely different properties compared with virgin CPET. Thus, impact results can vary even qualitatively from polymer to polymer. Figure 10.9 shows a comparison of the impact strength of PVC and CPET microcellular foams. It can be seen that at a given relative density the CPET foams possess a higher impact resistance. The Gardner impact data presented should only be used for relative comparison of materials. The engineer and designer is warned against using these data in

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Figure 10.8 Gardner impact strength of CPET microcellular foams as a function of foam relative density. Note that specimens prepared at 5 MPa saturation pressure has significantly higher impact strength compared to those prepared at 3 or 4 MPa. There was carbon dioxide induced crystallisation of CPET at 5 MPa [13]

Figure 10.9 A comparison of Gardner impact data on PVC and CPET. The CPET microcellular foams retain a larger fraction of the impact strength of the virgin polymer compared to PVC microcellular foams [48]

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Handbook of Polymer Foams design, for the impact conditions in actual use are likely to be significantly different from the idealised conditions for the Gardner test.

10.4 Current Research Directions New insights and innovations continue to drive the field of microcellular foams forward. Holl [49, 50] discovered that the cell growth mechanism in solid-state process is selflimiting. Further, he identified a new triaxial tensile failure mechanism that contributes to cell nucleation in solid state [51]. Handa’s recent discoveries of retrograde vitrification [52] and stress-induced nucleation in solid-state [39] have added new dimensions to this evolving field.

10.4.1 Microcellular Materials for Construction Microcellular technology has evolved around thin-walled applications. Can the microcellular process be scaled up to make thick parts for load-bearing applications? In an effort aimed at producing lightweight and energy efficient panels for advanced panel systems for future housing construction, Nadella and co-workers [53] have produced 10 mm thick ABS sheets with 50% or higher, reduction in density. Their process is illustrated in Figure 10.10. The key difference from the batch process of Figure 10.1 is

Figure 10.10 Schematic of batch process modified to produce flat and thick microcellular foams. Specimens 10 mm thick with 50% density reduction have been produced from ABS using this process [53]

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Microcellular Foams that the foaming is done inside a heated press in order to keep the foamed specimen flat. The other key difference is that the time required for saturating the thick specimens is much higher compared to thin sheets (the saturation time increases as square of the thickness). A key focus of the research is to look for processing strategies to reduce the saturation time to make the process more cost-effective.

11.4.2 Open-Cell (Porous) Microcellular Foams Many applications are envisioned in the biomedical field for porous microcellular foams made from biocompatible or biodegradable polymers. For example, it is hypothesised that a polymer implant with surface layers that are porous with pores in the 20 to 30 μm range might elicit a better healing response compared to an implant with a solid surface [54]. Tissue engineering is another large area of application, where porous scaffolds are needed to support natural tissue regeneration and growth. Figure 10.11 shows a porous 85/15 poly (DL-lactide-co-glycolide) foam made by the pressure quench method using supercritical carbon dioxide [55]. Various research groups around the globe are involved in the investigation of microcellular open cell foams. These foams have significant use in tissue engineering and other biomedical applications. The primary techniques used to produce these materials are phase separation and supercritical CO2 microcellular foaming.

Figure 10.11 Scanning Electron Micrograph of 85/15 poly(DL-lactide-co-glycolide) foam produced using the pressure quench method. The samples was saturated at 35 °C at 15, MPa, respectively. The foam had a porosity (open-cell content) of 76% as measured by an air picnometer [55]

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Handbook of Polymer Foams Tang and co-workers [56] used pressure-induced phase separation in a supercritical fluid to produce micro and ultra microcellular porous polymer membranes. Image, chemical and calorimetric analysis from their study reveals that membranes prepared by a combination of pressure-induced phase separation and plasma polymerisation with ethylene, are easier to control and have better characteristics. Huang and co-workers [57] produced open cell microcellular polycarbonate hollow fibers in a custom co-rotating twin-screw extrusion system. Carbon dioxide was used at the blowing agent. An average cell density of 109-1010 cell/cm3 and cell size in the range of 5-10 μm were achieved. Roweton and Shalaby [58] used a continuous crystallisation induced microphase separation process to make open cell thermoplastic microcellular foams. They suggest relationships between morphology and modes of microphase separation based on thermal property studies of representative foams. Porous biodegradable structures for cell transplantation are one of the applications for open cell microcellular foams. Open cell microcellular polylactic acid and polyphosphoester foams have been studied by Lo and co-workers [59], for cell culturing applications. They used the phase separation technique to produce a porous structure that allows dispersion of drugs and nutrients to the cells attached to the foam interior. Studies on thermally induced phase separation and gelation of rod shaped macromolecules to generate microcellular materials were conducted by Jackson and Shaw [60]. Low density materials were achieved by cooling the dilute isotropic solutions till phase separation and solvent freezing occurred. Cell sizes in the range of 1– 10 μm with cell walls 0.2 to 2.0 μm thick were reported. They also presented observations and theories explaining the underlying mechanism. Rodeheaver and Colton [61] experimented with the supercritical CO2 method to produce open cell microcellular polystyrene foam. Using saturation pressures above 17 MPa, foaming temperatures around 200 ºC and a scaled foaming time between 1 and 2 seconds they produced PS foam samples with 1 μm open cell pores. The resulting foam had both internal and surface porosity.

10.4.3 Sub-Micron Foams and Nanofoams When a crystallised PET specimen is foamed by the solid-state batch process using carbon dioxide, it is found that it has many orders of magnitude higher bubble density, and much smaller bubbles compared to amorphous PET [62]. Figure 10.12 shows an example of what some have termed ultramicrocellular foams - foams with cells in the range 0.11 μm. In this case we have a significant reduction in density of 26%, due to a very high cell nucleation density. Although this system is known to crystallise during the gas saturation step, the link between crystallites and the high nucleation density has not yet been established.

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Figure 10.12 Scanning electron micrograph of an ultramicrocellular CPET foam of 0.74 relative density. The average cell size is approximately 0.4 micrometers, and the cell density is estimated to be 1013 cells per cm3

Nanofoams - foams with pore sizes in the range of nanometers - are in concept an extension of microcellular foams. The idea of creating nano-scaled cells in polymeric materials is exciting and largely unexplored. Due to the unique structures, nanofoams are expected to have many properties that are superior to those of existing materials, such as much higher strength-to-weight ratios. It is expected that nanofoams would provide novel functional materials that could be tailored for the properties needed, for example, thermal conductivity, dielectric constant, acoustic and damping coefficients. Nanofoams have the potential to be used for any applications where foamed polymers are currently used, with possibly improved performance. These novel materials are expected to find a wide range of applications in construction, packaging, motor vehicle, microelectronics, and household products. In microelectronic devices, one of the potential application areas for nanofoams, the speed of pulse propagation is inversely proportional to the square root of the dielectric constant of the medium. Decreases in the dielectric constant of the insulator materials translate directly into improvements in microchips’ cycle time. In today’s microelectronics industry, the standard dielectric material used is SiO2, which becomes conductive when the clock speed of the chips becomes very high. It is therefore not a good enough insulator to prevent ‘cross talk’ between the closely spaced copper wires of the latest generation of semiconductors [63-65]. As chip-making technology advances from the current 0.18 mm

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Handbook of Polymer Foams lines to 0.13 mm and to 0.10 mm, there is an urgent need for new materials with much lower dielectric constants. Foamed materials possess air bubbles that have a very low dielectric constant of one. In order for foamed material to be used in microelectronics, the size of the air bubbles inside the polymeric materials must be smaller than the film thickness or any microelectronics features. The higher the volume fraction of the air bubble, the lower the dielectric constant. High volume fraction nanofoams have the potential to become the dielectric material in the next generation of microelectronic devices with much higher clock speed. The processing technique of polymeric nanofoams is currently very limited. Nanofoams have only been produced using a block copolymer method for microelectronics applications [64, 66]. In this method, the copolymer consists of thermally stable and thermally labile blocks. Upon heating, the thermally labile block undergoes thermolysis, leaving pores the size and shape of which are commensurate with the initial copolymer morphology. High thermally stable nanofoams have been produced with a low dielectric constant. However, the nanofoams produced have only 15-25% volume void fraction. The block copolymer method is also expensive and often requires chemicals that are environmentally hazardous. Polyimide nanofoams and their mechanical behaviour have been studied by Hilborn and co-workers [67] and Carter and co-workers [68]. More recently, Krause and co-workers [69] have reported open nanoporous morphologies based on carbon dioxide foaming. The research microcellular and nanocellular materials and their characterisation will benefit from advances in measurement of glass transition at the nano scale [70] and development of x-ray microtomography techniques for three-dimensional imaging of foam structure [71, 72]. To create nanofoams we have to achieve many orders of magnitude higher cell nucleation rates than realised to date. Experience with the microcellular process has shown that bubble nucleation density is exponentially related to gas concentration in polymers [6, 9]. Figure 10.13 shows the cell nucleation density in PS as a function of nitrogen saturation pressure. Over the range of nitrogen pressures explored, the number of cells nucleating increases exponentially with gas saturation pressure. The higher the gas saturation pressure, the more the gas will be dissolved in the polymer. Thus, the cell nucleation density is directly related to the amount of gas dissolved in the polymer. Recently, in a departure from convention, Handa and co-workers [52] have proposed a novel approach to achieving higher gas concentrations in polymers that is based on the phenomenon of retrograde vitrification described in Section 10.4.3.1.

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Figure 10.13 Cell nucleation density, cells per cm3, as a function of the gas saturation pressure in nitrogen-polystyrene system [6]. The number of cells nucleated is seen to increase exponentially with the gas saturation pressure

10.4.3.1 Phenomenon of Retrograde Vitrification To produce nanofoams, it is desirable to have high gas solubility and diffusivity. However, these are two conflicting objectives based on conventional wisdom. It is well known that the solubility of gases in polymers decreases with temperature and increases with pressure. It is also known that the diffusivity increases with temperature. In some gas-polymer systems, the diffusivity can be a strong function of gas pressure. Figure 10.14 shows the diffusion coefficients of CO2 in poly (methyl methacrylate) (PMMA) at temperatures below the Tg of PMMA. At low pressures (below about 2.7 MPa), the diffusion coefficient is higher at a higher temperature. At higher pressures, however, it is interesting to see that the gas diffusivity grows exponentially [52]. The observed phenomenon in Figure 10.14 is quite unusual. In the figure, the pressure at which the sharp change in diffusion coefficient occurs can be defined as the glass transition pressure, above which the polymer will transit from the glassy state to the rubbery state. When the glass transition pressures are plotted against the corresponding temperatures, as shown in Figure 10.15, it can be seen that for a given pressure, there are two glass transitions, which is contrary to the conventional knowledge of polymers. The high Tg is what has been usually observed. The low Tg is where the polymer transit from rubbery state to glassy state with heating. This phenomenon was first found by Condo and Johnson,

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Figure 10.14 Diffusion coefficients of CO2 in PMMA as a function of the gas saturation pressure at temperatures below the Tg of neat PMMA [ 52]

Figure 10.15 The glass transition temperature of the CO2 - PMMA system as a function of the gas saturation pressure showing the retrograde vitrification phenomenon [52]

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Microcellular Foams in 1992 in a theoretical study on the glass transition behaviour of polymers with compressed fluid diluents [73]. It was later verified experimentally [52, 74]. Due to the fact that the glass transition can result from increasing the temperature, rather than decreasing the temperature, this phenomenon is termed ‘retrograde vitrification’. Retrograde vitrification is a consequence of the complex effects of temperature and pressure on the gas sorption process. At a constant pressure in this retrograde region, sorption increases with a reduction in temperature, thus causing a glass-to-rubber transition. This phenomenon has opened a new avenue for polymer processing under milder conditions, because it allows polymers to be plasticised with compressed gas under much lower pressures and temperatures. A low-temperature foaming process has recently been developed by Handa and Zhang [75] for the CO2-PMMA gas-polymer system. The polymer PMMA is first saturated in CO2 at 0 °C and 3.4 MPa. After the PMMA is fully saturated, the pressure is slowly released. Then the polymer-gas solution is quickly heated to 80 °C. The importance of the low temperature process is that a high gas solubility can be achieved at low temperatures and low pressures, which is essential in generating very small cells and high cell densities. Furthermore, the diffusion coefficient at low temperature can be the same as at higher temperatures such that the gas saturation process at temperatures below the retrograde vitrification temperature is as fast as that at higher temperatures. Using this process, ultra-microcellular foams with closed cells as small as 0.35 μm and cell density as high as 4.4 x 1013 cells/g have been produced [52].

10.5 Commercial Opportunities Over the past 20 years since microcellular foams were first invented many groups around the world have spent considerable research effort to design and develop viable industrial manufacturing processes for these materials. Initial efforts on developing an extrusion process did not yield the expected results due to numerous technical difficulties. To begin with, the gas had to be injected at supercritical pressures due to the low solubility of gas at melt temperatures. Another challenge was that gas injection into the polymer melt yielded a two-phase mixture in the barrel. For microcellular foaming to occur it is important for the gas and polymer to be in a one-phase solution. This problem of going from a two phase mixture to a one phase solution is not trivial. Die design to obtain an acceptable surface finish was another challenge as surface bubbles affected the surface finish. Moreover, these design changes were found to be polymer specific. A further difficulty in extrusion process development was arresting bubble growth beyond the desired micro-scale at the die exit. To the best of our knowledge, PS is the only polymer for which microcellular extrusion has been successfully commercialised.

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Handbook of Polymer Foams The semi-continuous process described earlier has been slow to get attention due to the perception that gas saturation into the polymer roll takes too long for the process to be commercially viable. Major strides in commercialising microcellular foams have been made with the development of the microcellular injection moulding process. Trexel, Inc., of Woburn, MA, USA has successfully developed and licensed microcellular injection moulding technology to processors around the world [29]. Teaming up with equipment manufacturers like Milacron, Trexel is designing and marketing microcellular attachments for standard injection moulding machines. Numerous applications are envisioned for microcellular foams. Current efforts towards commercialisation are focused on automotive, construction, food packaging, and industrial foams markets. Microcellular parts made using injection moulding have diverse applications in markets such as business equipment, automotive, electrical, precision trays, encapsulated products, etc. Examples of these applications are internal printer components in business equipment market, under dash components, housings and power train components in automotive market. Microcellular automotive liners, house siding panels (exterior panel finished with a plastic sheet) and vinyl window profiles are some of the products that can be made in an extrusion process. Thermoformed disposable food packaging, building interior cushion (carpet underlay) and industrial foam applications are areas where microcellular foams made by the semi-continuous process can be used. Examples of such products are clamshells (disposable food container with a hinge), carpet cushion and marine pads (a floating product used as a marker). Although commercialisation of microcellular foams has been slow so far, we believe that with continuing worldwide efforts to address the manufacturing challenges, the next decade will see the potential of these novel materials realised in many areas.

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V. Kumar, Process Synthesis for Making Microcellular Thermoplastic Parts: A Case Study in Axiomatic Design, Department of Mechanical Engineering, MIT, USA, 1988. [Ph.D. Thesis]

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10. R.E. Murray, J.E. Weller and V. Kumar, Cellular Polymers, 2000, 19, 6, 413. 11. V. Kumar and O.S. Gebizlioglu, Proceedings of SPE Antec 92, Detroit, MI, USA, 1992, 1536. 12. Y.P. Handa, B. Wong, Z. Zhang, V. Kumar, S. Eddy and K. Khemani, Polymer Engineering and Science, 1999, 39, 1, 55. 13. V. Kumar, R.P. Juntunen and C. Barlow, Cellular Polymers, 2000, 19, 1, 25. 14. V. Kumar and J.E. Weller, International Polymer Processing, 1993, 8, 1, 73. 15. V. Kumar and J.E. Weller, Polymer Engineering and Science, 1994, 34, 3, 169. 16. S.K. Goel and E.J. Beckman, 1993, Cellular Polymers, 1993, 12, 4, 251. 17. K.A. Arora, A.J. Lessor and T.J. McCarthy, Macromolecules, 1998, 31, 14, 4614. 18. A. Cooper, Journal of Materials Chemistry, 2000, 10, 2, 207. 19. V. Kumar, and H.G. Schirmer, Proceedings of SPE Antec 95, Boston, MA, USA, 1995, Volume 2, 2189. 20. V. Kumar and H.G. Schirmer, inventors; University of Washington, assignee; US5,684,055, 1997, 21. G. Branch, Design of Lab-Scale Machine for Semi-Continuous Production of Microcellular Foams, Department of Mechanical Engineering, University of Washington, USA, 2001. [M.Sc. Thesis]

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Handbook of Polymer Foams 22. C.B. Park and N.P. Suh in Proceedings of the ASME Winter Annual Meeting, Anaheim, CA, USA, MD Series, 1992, Volume 38, 69. 23. C.B. Park, A.H. Behravesh and R.D. Venter, Polymeric Foams: Science and Technology, Ed., K.C. Khemani, ACS Symposium Series No.669, ACS, Washington, DC, USA, 1997, 115. 24. M. Shimbo, K. Nishida, S. Nishikawa, T. Sueda and M. Eriguti, Porous, Cellular and Microcellular Materials, Ed., V. Kumar, MD Series, ASME, 1998, Volume 82, 93. 25. B. Seibig, Q. Huang and D. Paul, Cellular Polymers, 2000, 19, 2, 93. 26. V. Kumar and N.P. Suh, Polymer Engineering and Science, 1990, 30, 20, 1323. 27. K.A. Seeler, S.A. Billington, B.D. Drake and V. Kumar, in Cellular and Microcellular Materials, MD series, ASME, 1996, Volume 76, p.65. 28. K.A. Seeler, S.A. Billington, B.D. Drake and V. Kumar, Proceedings of SPE Antec 97, Toronto, Canada, 1997, Volume 2, 2032. 29. D. Bernstein, Proceedings of SPE FOAMS 2002 conference, Houston, TX, USA, 2002, Keynote lecture. 30. A.N. Gent and D.A. Tompkins, Journal of Applied Physics, 1969, 40, 6, 2520. 31. J.H. Saunders and R. Hansen, The Mechanism of Foam Formation, Plastic Foams, Eds., K.C. Frisch and J.H. Saunders, Marcel Dekker, New York, NY, USA, 1972, 39. 32. A. Afremanesh and S.G. Advani, Proceedings of the Symposium on Processing of Polymers and Polymeric Composites, ASME Winter Annual Meeting, 1990, MD Series, Volume 19, 185. 33. A. Arefmanesh and S.G. Advani in Proceedings of the ASME International Mechanical Engineers Congress and Expo, Porous, Cellular and Microcellular Material, Eds., V. Kumar and S.G. Advani, Orlando, FL, USA, MD Series, 1992, Volume 38, 25. 34. N.S. Ramesh and N. Malwitz in Polymeric Foams: Science and Technology, Ed., K.C. Khemani, ACS Symposium Series No.669, ACS, Washington, DC, USA, 1997, 115.

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Microcellular Foams 35. N.S. Ramesh in Porous, Cellular and Microcellular Materials, Ed., V. Kumar, Proceedings of the ASME International Mechanical Engineers Conference, Anaheim, CA, USA, MD Series, Volume 82, 1998, 71. 36. M. Wessling, Z. Borneman, T. Van Den Boomgaard and C.A. Smolders, Journal of Applied Polymer Science, 1994, 53, 11, 1497. 37. J.H. Aubert and R.L. Clough, Polymer, 1985, 26, 13, 2047. 38. A.T. Young, Journal of Cellular Plastics, 1987, 23, 1, 55. 39. Y.P. Handa and Z. Zhang, Cellular Polymers, 2000, 19, 2, 77. 40. V. Kumar, M. VanderWel, J.E. Weller and K.A. Seeler, Journal of Engineering Materials and Technology, 1994, 116, 439. 41. L.J. Gibson and M.F. Ashby, Cellular Solids, Structure and Properties, 2nd Edition, Cambridge University Press, Cambridge, UK, 1999. 42. W. Albrecht, Cellular Polymers, 2000, 19, 5, 319. 43. M.J. Williams and A.D. Wrobleski, Journal of Materials Science, 1989, 24, 11, 3799. 44. V. Kumar and K.A. Seeler, Proceedings of SPE Antec 93, New Orleans, LA, USA, 1993, Volume 2, 1823. 45. G. Wing, A. Pasricha, M. Tuttle and V. Kumar, Polymer Engineering and Science, 1995, 35, 8, 673. 46. W.D. Armstrong and V. Kumar, Journal of Polymer Science: Polymer Physics Edition, 2000, 38, 5, 691. 47. R.P. Juntunen, V. Kumar, J.E. Weller and W.R. Bezubic, Journal of Vinyl and Additive Technology, 2000, 6, 2, 93. 48. V. Kumar, Proceedings of the SPE Antec 2002, San Francisco, CA, USA, 2002, 1892. 49. M.R. Holl, Dynamic Analysis, Measurement, and Control of Cell Growth in Solid State Polymeric Foams, Department of Mechanical Engineering, University of Washington, 1995. [Ph.D. Thesis]

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Handbook of Polymer Foams 50. M.R. Holl, J. Garbini, W.R. Murray and V. Kumar, Journal of Polymer Science: Polymer Physics Edition, 2000, 39, 8, 868. 51. M.R. Holl, V. Kumar, J.L. Garbini and W.R. Murray, Journal of Materials Science, 1999, 34, 3, 637. 52. Y. P. Handa, Z. Zhang and B. Wong, Cellular Polymers, 2001, 20, 1, 1. 53.

V. Kumar, K. Nadella and W. Li, Proceedings of SPE Antec, Nashville, TN, USA, 2003, p.1722-1726.

54. V. Kumar in Porous, Cellular, and Microcellular Materials, Ed., V. Kumar, Proceedings of the ASME Mechanical Engineers Congress, Anaheim, CA, USA, MD Series, Volume 82, 1998, 5. 55. L. Singh, V. Kumar and B.D. Ratner, Porous, Cellular, and Microcellular Materials, Ed. V. Kumar, Proceedings of the ASME International Mechanical Engineers Congress and Expo, Orlando, FL, USA, MD Series, Volume 91, 2000, 29. 56. C. Tang, L. Xu and C. Li in Proceedings of the SPIE 2nd International Conference on Thin Film Physics and Applications, Eds., S. Zhou, Y. Wang, Y. Chen and S. Mao, 1994, Volume 2364, 603. 57. Q. Huang, B. Seibig and D. Paul, Journal of Cellular Plastics, 2000, 36, 2, 112. 58. S. Roweton and S.W. Shalaby, Transactions of the Annual Meeting of the Society for Biomaterials in Conjunction with the International Biomaterials Symposium, Toronto, Canada, 1996, Volume 2, 95. 59. H. Lo, S. Kadiyala, S.E. Guggino and K.W. Leong, in Biomaterials for Drug and Cell Delivery, Eds., A.G. Mikos, R.M. Murphy, H. Bernstein and N.A. Peppas, Materials Research Society Symposium Proceedings, Volume 331, 1993, 41. 60. C.L. Jackson and M.T. Shaw, Polymer, 1990, 31, 6, 1070. 61. B.A. Rodeheaver and J.S. Colton, Polymer Engineering and Science, 2001, 41, 3, 380. 62. V. Kumar and P.J. Stolarezuk, Proceedings of SPE Antec ‘96, Indianapolis, IN, USA, 1996, Volume 2, p.1894. 63. M. McCoy, Chemical and Engineering News, 2001, 79, 47, 43.

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Microcellular Foams 64. J.L. Hedrick, K.R. Carter, H.J. Cha, C.J. Hawker, R.A. DiPietro, J.W. Labadie, R.D. Miller, T.P. Russell, M.I. Sanchez, W. Volksen, D.Y. Yoon, D. Mecerreyes, R. Jerome and J.E. McGrath, Reactive and Functional Polymers, 1996, 30, 1-3, 43. 65. J.S. Fodor, R.M. Briber, T.P. Russell, K.R. Carter, J.L. Hedrick, R.D. Miller and A. Wong, Polymer, 1999, 40, 10, 2547. 66. J.E. McGrath, S.K. Jayaraman, P. Lakshmanan, J.C. Abed and F. Afchar-Taromi, 1996, Proceedings of the ACS Meeting, New Orleans, LA, USA, 1996, p.136. 67. Y. Leterrier, J-A.E. Manson, J.G. Hilborn, C.J.G. Plummer and J.L. Hedrick, Advances in Porous Materials, Eds., S. Komarneni, D.M. Smith and J.S. Beck, Materials Research Society Symposium Proceedings, Volume 371, 1995. 68. K.R. Carter, J.L. Hedrick, R. Richter, P.T. Furuta, D. Mecerreyes and R. Jerome in Microporous and Macroporous Materials, Eds., R.F. Lobo, J.S. Beck, S.L. Suib, D.R. Corbin, M.E. Davis, L.E. Iton and S.I. Zones, Materials Research Society Symposium Proceedings, Volume 431, 1996, 487. 69. B. Krause, K. Diekmann, N.F.A. Van Der Vegt and M. Wessling, Macromolecules, 2002, 35, 5, 1738. 70. R.M. Overney, C. Buenviaje, R. Luginbuehl and F. Dinelli, Journal of Thermal Analysis and Calorimetry, 2000, 59, 205. 71. G.T. Seidler, L.J. Atkins, E.A. Behne, U. Noomnarm, S.A. Koehler, R.R. Gustafson and W.T. McKean, Advances in Complex Systems, 2001, 4, 4, 481. 72. J.A. Elliott, A.H. Windle, J.R. Hobdell, G. Eeckhaut, R.J. Oldman, W. Ludwig, E. Boller, P. Cloetens and J. Baruchel, Journal of Materials Science, 2002, 37, 8, 1547. 73. P.D. Condo and K.P. Johnston, Macromolecules, 1992, 25, 24, 6730. 74. P.D. Condo, I.C. Sanchez, C.G. Panayiotou and K.P. Johnston, Macromolecules, 1992, 25, 23, 6119. 75. Y.P. Handa and Z. Zhang, inventors; no assignee; US5,955,511, 1999.

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268

Abbreviations

Abbreviations

ABA

Alternate blowing agent(s)

ABS

Acrylonitrile-butadiene-styrene

ACGIH

American Conference of Governmental Industrial Hygienists

ADC

Azodicarbonamide

AFPF

Alliance for Flexible Polyurethane Foams

API

Alliance for the Polyurethane Industry

APP

Aromatic polyester polyol(s)

ASTM

American Society for Testing and Materials

BHT

Butylated hydroxy toluene

BP

Boiling point

BR

Butadiene rubber

BS

British Standard

CAA

Civil Aviation Authority

Cal TB

California Technical Bulletin

CBA

Chemical blowing agent(s)

CEFIC

European Chemical Industry Council

CFC

Chlorofluorocarbon(s)

CFC-11

Chlorofluorocarbon-11

CFC-114

1,1-Dichloro,1,2,2,2-tetrafluoroethane

CFC-12

Chlorofluorocarbon-12

CFD

Compression force deflection

CFR

Code of Federal Regualtions

CO2

Carbon dioxide

CONEG

Coalition of Northeastern Governors

C-PAT

Quasi-continuous form pressure and temperature system

269

Handbook of Polymer Foams CPET

Crystallisable PET

DCP

Di-cumyl peroxide

DEG

Diethylene glycol

DIDP

Di-isodecyl phthalate

DIN

Deutsches Institut für Normung (German Institute for Standardisation)

DMEA

Dimethyl ethanolamine

DMT

Di-methyl terephthalate

DOE

US Department of Energy

DPB

Dimethylether/propane/butane

DPG

Diphenyl guanidine

EMA

Ethylene methyl acrylate

EO

Ethylene oxide

EPA

US Environmental Protection Agency

EPDM

Ethylene-propylene diene terpolymer

EPP

Expanded polypropylene

EPS

Expanded polystyrene

EU

European Union

EVA

Ethylene vinyl acetate

FAA

Federal Aviation Authority

FAR

Federal Aviation Regulations

FDA

Food and Drug Administration, USA

FKS

Vereniging van Fabrikanten van Kunststofleidingsystemen (The Dutch Federation of Plastic Pipe System Manufacturers)

FMVSS

Federal Motor Vehicle Safety Standard

FPF

Flexible polyurethane foam

GCD

Gaseous carbon dioxide

GRAS

Generally regarded as a safe

GWP

Global warming potential

HA

High ammonia

HBCD

Hexabrominated cyclodecane

HBFC

Hydrobromofluorocarbons

HC

Hydrocarbon(s)

HCFC

Hydrochlorofluorcarbon(s)

270

Abbreviations

HCFC-124

Tetrafluroethane

HCFC-141b

Dichlorofluoroethane

HCFC-142b

1-Chloro-1,1, diflurorethane

HCFC-22

Chlorodifluoromethane

HDPE

High density polyethylene

HFC

Hydrofluorocarbon(s)

HFC-134a

1,1,1,2-Tetrafluoroethane

HFC-152a

1,1-Difluoroethane

HFC-227ea

1,1,1,2,2,3-Heptafluoropropane

HFC-245fa

1,1,1,3,3-Pentafluoropropane

HFC-365mfc

1,1,1,3,3-Pentafluorobutane

HFE-245

Pentafluoro methyl ether

HFE-254mf

2,2,2, Trifluoroethyl difluoro methyl ether

HFE-356

Hexafluoroethane

HR

High resilience

ICF

Insulated concrete form

IFD

Indentation force deflection

III

International Isocyanate Institute

IR

Infra red

ISOPA

European Isocyanate Producers Association

JAA

Joint Aviation Authorities

JAR

Joint Aviation Regulations

JIS

Japanese Industrial Standard

JUFA

Japan Urethane Foam Association

L/D

Length:diameter ratio

LA

Low ammonia

LCD

Liquid carbon dioxide

LDPE

Lowdensity polyethylenen

LLDPE

Linear low density polyethylene

MDI

Methylene diphenyl diisocyanate

MDPE

Medium density polyethylene

MMDI

Di-cyclic monomeric MDI

mPE

Metallocene catalysed polyethylene(s)

271

Handbook of Polymer Foams MSDS

Material safety data sheet

MST

Mechanical stability time

MVSS

Motor Vehicle Safety Standard

N/A

Not available

N2

Nitrogen

NIH

National Institute of Health

NR

Natural rubber

OBSH

Oxybisbenzenesulfonyl hydrazide

ODP

Ozone depletion potential

ODS

Ozone depleting substance(s)

OEL

Occupational Exposure Limit as measured by manufacturer

OSHA

Occupational Safety & Health Association

PA

Phthalic acid

PAT

Pressure and Temperature System

PBA

Physical blowing agent(s)

pbw

Parts by weight

PC

Polycarbonate

PET

Polyethylene terephthalate

PETG

Glycol-modified PET

PFA

Polyurethane Foam Association

PHD

Polyharnstoff (polyurea) dispersion

phr

Parts per hundred rubber

PIR

Polyisocyanurate

PMDI

Polycyclic polyisocyanates

PMMA

Polymethyl methacrylate

POE

Polyolefin elastomer(s)

POP

Polyolefin plastomer(s)

PP

Polypropylene

pph

Parts per hundred

PPSO

Polyphenylene sulfoxide

PS

Polystyrene

PS

Polystyrene

PU

Polyurethane(s)

272

Abbreviations

PURRC

Polyurethane Recycle and Recovery Council

PVC

Polyvinyl chloride

PVC-U

Unplasticised PVC

RC

Latex foam rubbers, cored

RH

Relative humidity

rpm

Revolutions per minute

RU

Latex foam rubbers, uncored

SAN

Styrene acrylonitrile

SBC

Sodium bicarbonate

SBR

Styrene-butadiene rubber

SELCHP

South-East London Combined Heat and Power Consortium

SI

Statutory Instrument

SOLAS

International Convention for the Safety of Life at Sea

SP

Styrenated phenol

SPI

Society of the Plastics Industry

S-PVC

Suspension polyvinylchloride

STP

Standard, temperature and pressure

TCFM

Trichlorofluoromethane

TCPP

Tris monochloro isopropyl phosphate

TDCP

Tris dichloro isopropyl phosphate

TDI

Toluene diisocyanate

Tg

Glass transition temperature

TLV

Threshold Limit Value

TMP

Trimethylol propane

TPE

Thermoplastic elastomer(s)

TPU

Thermoplastic polyurethanes(s)

TSH

p-Toluenesulfonylhydrazide

TSS

p-Toluenesulfonylsemicarbazide

UNEP

United Nations Environmental Programme

UV

Ultraviolet

VLDPE

Very low density polyethylene

VOC

Volatile organic compounds

VPF

Variable pressure foaming

273

Handbook of Polymer Foams WEEE

Waste electrical and electronic equipment

XPS

Extruded polystyrene

ZDC

Zinc diethyl dithiocarbonate

ZMBT

Zinc salt of mercapto benzthiazole

ZOT

Zinc oxide thickening test

ZST

Zinc oxide viscosity test

274

Contributors

Andrew Barnetson British Plastics Federation, 6 Bath Place, Rivington Street, London, EC2A 3JE

David Eaves The Barns, Station Road, Harbury, Warwickshire, CV33 9HQ

Christopher Howick European Vinyls Corporation (UK) Ltd, The Heath, Runcorn, Cheshire, WA7 4QF

Tyler Housel Inolex Chemical Company, Jackson and Swanson Streets, Philadelphia, PA 19148, USA

Rani Joseph Department of Polymer Science and Rubber Technology, Cochin University of Science and Technology, Kochi - 682022, Kerala, India

Vipin Kumar Department of Mechanical Engineering, University of Washington, Seattle, Washington 98195, USA

Krishna Nadella Department of Mechanical Engineering, University of Washington, Seattle, Washington 98195, USA

Sachchida Singh Huntsman Polyurethanes, 286 Mantua Grove Road, West Deptford, NJ 08066-1732, USA

Noreen Thomas Institute of Polymer Technology and Materials Engineering, University of Loughborough, Loughborough, Leicestershire, LE11 3TU

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Handbook of Polymer Foams

276

Author Index A

E

Arefmanesh, A. 249 Ashby, M.F. 6, 250 Ashford, P. 79

Eaves, D. 1, 55, 173

B Ball, G.W. 77, 78 Barnetson, A. 37 Beckmann, G. 126, 127, 128, 129 Bertucelli, L. 69 Birch, S.J. 165 Branch, G. 248 Brenis, K.L. 132

G Gale, M. 125, 137 Gent, A.N. 249 Gibson, L.J. 250 Gibson, W. 6 Glicksman, L.R. 6

H

Carter, K.R. 258 Collington, K.T. 189 Colton, J.S. 246, 256 Condo, P.D. 259 Cousins, J.R. 178, 179 Cunningham, A. 6

Han, C.O. 125 Handa, Y.P. 249, 254, 258, 261 Hansen, R.H. 125 Hilborn, J.G. 258 Holl, M.R. 254 Hooke, R. 3 Housel, T. 85 Howick, C.J. 155 Huang, Q. 256 Hughes, R. 124

D

I

Decker, R.W. 141 Dey, S.K. 137 Dobrowsky, J. 124 Domas, F. 178

Ide, F. 138

C

J Jackson, C.L. 256 Johnson, K.P. 259 Joseph, R. 207

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Handbook of Polymer Foams

K Kaufung, R. 79 Kim, B.C. 131, 132 Krause, B. 258 Kumar, K. 243 Kumar, V. 246, 247, 249 Kweeder, J.A. 246

L Landrock A.H. 58 Lo, H. 256

M Mack, M.H. 177 Maier, R.D. 184 Meyke, J. 177 Molina, M. 15 Murphy, E.H. 229

N Nadella, K.V. 243, 254 Niven, W.G. 157

Rodeheaver, B.A. 256 Ross, M. 138 Roweton, S. 256 Rowland, F. 15

S Sarvetnick, H.A. 157 Saunders, J.H. 249 Schirmer, H.C. 247 Seeler, K.A. 249 Seibig, B. 249 Shalaby, S.W. 256 Shaw, M.T. 256 Shimbo, M. 249 Singh S.N. 9 Suh, N.P. 249 Szamborski, G. 138, 140

T Talalay, A. 231 Tang, C. 256 Thomas, N.L. 123, 132 Throne, J.L. 143 Tideswell R.B. 60

O Okano, K. 138

P Park, C.B. 249 Patterson, J. 124, 140 Pfennig, J-L. 138 Puri, R.R. 189

R Rabinovitch, E.B. 131, 132 Ramesh, N.S. 249

278

W Weigand, E. 79 Williams, M.J. 251 Wrobleski, A.D. 251

Z Zhang, Z. 249, 261 Zipfel, L. 69

Company Index A

F

ARC 82

Furukawa Electric Co. 181, 182, 183, 186

B BASF AG 37, 45, 46, 54, 76, 177, 178, 179 Bayer AG 75, 79, 82 Beamech 100, 101, 102 Berstorff GmbH 176, 177, 179 BFGoodrich Sponge Products 231 Borealis 177, 184 BP 54

G Goldschmidt 73

H Hennecke GmbH 75 Hitachi 182, 183, 186 Hitachi Chemical Co. 181

C

I

Celotex Corporation 73 Congoleum Corporation 167, 168

IBM 38

K D Dex Plastomers 184 Dow 184 Dunlop 207, 208, 232 Dupont Dow 184 Dynisco 137

E Elenac 184 Exxon 184

Kodak 38

M Matheson 137 Meccano Toy Company 38 Montell 177, 179

N Nitroil 72 Nova Chemicals Corporation 54

279

Handbook of Polymer Foams

P Phillips 184 Puren Schaumstoffe 76

R Reifenhauser GmbH 176

S Sekisui Electrical Co. 180, 186, 190 Solvay 69

T Trexel Inc. 249, 262

Z Zotefoams plc 189, 192, 195, 196, 197, 198

280

Subject Index A ABS microcellular foams 246 Accelerator dispersions formulations 210 Additives anti-static 94 biocides 94 clickability 94 plasticisers 94 Anisotropy 2 Antioxidant emulsion formulation for 211 Appliance insulation 67 Aromatic polyester polyols 59, 60 Azodicarbonamide blowing agent 165

B Blend compatiblisers 73 Blowing agents 9, 175 acetone 24 alcohol 24 alternative 66, 97 application 25, 26, 27 azo compounds 30 azodicarbonamide 31, 133, 134, 135, 136, 156, 159, 174, 185 bicarbonates/carbonates 32 blends of physical 24 carbon dioxide 10, 22, 23, 24, 97, 174

CFC 174 characteristics of 66 chemical 25, 28, 29 chemical inhibition 167 dichlorodifluoromethane 62 dihydrooxadiazinone 33 encapsulated physical 25 endo/exo blends 33 endothermic 32 environmental acceptability 11 fluorinated ethers 24 fluoroiodocarbons 24 foam type 25, 26, 27 global warming 11 HCFC 174 health impacts of 11 hydrazine derivates 31 hydrocarbons 174 inert gases 22 inert 175 liquefied CO2 97 methyl chloride 14 methyl chloroform 24 methylene chloride 14 n-nitroso compounds 32 n-pentane 68, 69 nitrogen 22, 23, 24, 174 oxybisbenzenesulfonyl hydrazide 133 oxygen 22 ozone depletion 11 physical 10, 24, 25, 26, 27 polycarboxylic acid derivatives 33 polyphenylene sulfoxide 32

281

Handbook of Polymer Foams properties of 14 selection criteria for physical 10 sodium bicarbonate 133, 134, 135, 136 solubility of the physical 12 sulfonyl semicarbazides 31 supercritical fluid 23 tetrazoles 33 trichlorofluoromethane 62 vapour pressure 12 water 24 Blown foams carbon dioxide water 68 Bubble nucleation 245, 246

C Carpets foamed PVC backings 168 Catalysts blow 91 delayed 91 gel 91 metallocene 174 potassium hydroxide 57 potassium salts 71 quaternary ammonium salts 71 reactive 92 tertiary amines 71 tin 72 tin compounds 71 Cell openers 72 Cell shape 3 Cell size 2, 107 Cell uniformity 107 Celuka process 126, 136, 143 Chemical blowing agents exothermic 30 polyvinyl chloride 29 thermoplastics processing 29

282

Chlorofluorocarbons 7, 13 chemical stability 15 properties of 14 solubility 15 trichlorofluoromethane 13 Closed cell foam 12, 13 Compression force deflection 105 Compression modulus 105 Core pipe PVC foam 142 Cushion packaging 5 Cushion vinyl floorings 167, 168

D Dunlop process 207, 208, 217, 231, 232 fillers 219 flame resistance 219 foam stabilisers 218, 219 gelling 220 softeners 219 stabilisers 220 Durometer 105

E Expanded polystyrene 37 applications 43 automotive industry 44 bead 38, 39 chemical properties 46 construction 42, 43 construction industry 37 conversion of bead to product 39 cycle helmets 44 development of 37 energy recovery 53 European market 47 European production 48 final moulding 40

Subject Index fire retardants 50 floating pontoons 43 fruit and vegetable packing 46, 47 garden containers 42 global structure of markets 47 incineration 53 insulated concrete form 44 insulation 41 landfill 53 major manufacturers 54 maturing 40 mechanical performance 45 mechanical recycling 53 mouldings 38 packaging 41 physical properties 45, 46 pre-expansion 39 pre-foamers 39 production in Asia 48, 49 production in USA 49 properties 46 properties of 44 recycling 51, 52 Regional Trade Associations 54 smoke 50 surf boards 44 underfloor insulation 45 wall insulation 45 Expanded polystyrene packaging applications 41 Expanding fillers 25 Extruded sheet chemically crosslinked 181, 182, 183 irradiation crosslinked 180, 181

F Filler slurry formulation for 211 Fillers

chalk 162 mineral fillers 162 Flame retardant hexabrominated cyclododecane 50 Flexible PVC foams suspension PVC 155 Flexible polyurethane foams 5, 85 additives 94 adhesion promoters 94 antioxidants 92 blow reaction 86 blowing gas 97 carpet cushion 110 catalyst 91 cell growth 96 cell nucleation 96 cell opening 97, 98 cell structure 107 chamber pressure 96 characterisation 104 chemistry 85 colorants 92 comfort 110 compression set 108 cure 98, 99, 101 density 104 environmental issues 111 environmental stability 107 fatigue 108 flame retardants 93 flammability 108, 109 foam rise 101 foaming process 94 gel reaction 86 hardness 104, 105 isocyanate 88 light stabilisers 93 manufacturing equipment 99 markets 109 methylene diphenyl diisocyanate 88

283

Handbook of Polymer Foams mixing 95, 96, 101 moulded 85 packaging 111 polyol 88, 89 porosity 106 production in 2001 109 raw material conditioning 95 recycling 113 resilience 105 slabstock 85 specialty applications 111 starting materials 87 surfactant 90 storage and delivery 100 strength properties 106, 107 toluene diisocyanate 88 transportation 110 water 90 Flexible PVC foams 155 blowing agent 165 blowing agents 159 cell types 160 closed cell 160, 161 dispersion 156 emulsion resins 162 foam formation 159 gelation 159 liquid plasticiser 163 open cell 160, 161 paste resin 156 pigments 163 plasticiser 164, 165 plastisol 155 Foam cladding co-extruded 130 Foam density 2, 139, 196 azodicarbonamide 136 concentration 134 blowing agent 139 processing aid 138, 139

284

SBC concentration 135 screw speed 132 Foam expansion kicker 159, 160 Foam extrusion 124 basic principles 125 Celuka method 126, 128, 129 free-foam sheet 127 free-foaming method 126 processes 126 Foam morphology 125 Foam polyol 89 Foam profile co-extruded 131 rigid PVC 141 Foam properties 3 compression 3 energy absorption 5 stress-strain curve 3, 4 Foam sheet rigid PVC 142 Foam specification aerospace 201 automotive 201 buoyancy 201 furnishings 201 packaging 200 Foam structure 1 gas bubbles 1 surface tension 1 viscous 1 Foamed plastisols carpet backings 166 cushion vinyl flooring 166 floorings 166 PVC leathercloth 169 synthetic leather 169 wallcoverings 168 Foamed PVC properties of 144

Subject Index Foams chemically blown 156 FPF environmental issues 112, 113 slabstock 100

G Gases inert 22 Glass fibre 73 Global warming potential 11, 20

H HC blowing agents cyclo-pentane 21 iso-pentane 21 isobutane 21 n-butane 21 n-pentane 21 propane 21 properties of 21 HCFC 15 ozone depleting potential 16 phase out schedule 18 HCFC blowing agents properties of 17 HFC blowing agents characteristics of 70 properties of 19 Hydrocarbons 20 halogenated 13 Hydrofluorocarbons 18

I Indentation force method 105 Insulation material Western European market 79 Isocyanate 60, 62, 85, 87

index 87

L Latex 217 ammonia content 216 high ammonia 215 low ammonia latex 215 thickening test 216 zinc oxide 216 zinc oxide viscosity test 216 zinc stability time 216 Latex compounds formulation 215 Latex foam 207 accelerator 210 antioxidant 211 batch process 209 bush moulds 214 compression set 236 curing 214 deammoniation 212 density 238 Dunlop process 208, 230 filler 211 flexing resistance 237 foaming 212 formulation 209 furniture 239 gelling 213 indentation hardness 237, 238 manufacture 216 maturation 212 metallic impurities 238 natural rubber 208 nitrile rubber 217 polychloroprene rubber 218 preparation 212 refining 213 Talalay mould 231, 233

285

Handbook of Polymer Foams testing 235 transportation 238 uses 238, 239 washing and drying 214 Latex foam manufacture troubleshooting 235 Latex foam production continuous process for 229

Montreal Protocol 15, 16, 18, 57, 62, 66, 81, 175 Moulded foam 101 Moulding machines 99 mPE commercial availability 184 MuCell process 146, 147

N M Maxfoam 102, 103 MDI composition of 61 Microcellular foam 23, 243 batch process 254 commercial opportunities 261 creep behaviours 251 extrusion processes 248, 249 fatigue 251 for construction 254 Gardner impact strength 251, 252, 253 nanofoams 256 open-cell 255 pressure-induced phase separation 256 pressure-quench method 246 processing of 244 properties of 249 relative density 250, 251 relative tensile strength 251 retrograde vitrification 259 semi-continuous process 247, 248 solid-state batch process 244, 245 sub-micron foams 256 supercritical CO2 256 temperature soak process 245 tensile property data 249 tensile strength 250 unfoamed skin 245, 247

286

Nanofoams 257, 258 carbon dioxide foaming 258 polyimide 258 Natural rubber latex 215 Neopolen P bulk density 179 moulded density 179 Neoprene 217 Nitrogen autoclave process blowing agent 192 cell size 192 crosslinking 192 expansion 192 foam cell structure 192

O Open cell foam 1 Open cell/closed cell ratio 2 Ozone depleting substances 65 consumption phase-out of 63, 64

P Pentane blown PIR foam properties of 77 Physical blowing agents carbon dioxide 137 nitrogen 137

Subject Index Plasticisers benzoates 163 butylbenzyl phthalate 163, 164 dialkyl phthalate esters 163 DIDP 163, 164 Plastisol gelation temperatures 165 lamination 170 Plastisol foam coating 157 expansion 158 formation 157 fusion 158 gelation 158 microsuspension resin 161 PVC resins 161 semi-gelation 157, 158 Polycarbonate microcellular foams 246 Polyester foams 94 Polyester polyols 58 Polyesters melting points of 60 Polyether foams 94 Polyether polyols 57 Polyethylene foam closed cell 5 Polyethylene terephthalate microcellular foams 246 Polyisocyanurate foams 57 fire resistance 60 Polymer foams extrusion of 125 Polyolefin foams 173 additives 185 aerospace 198 annual demand 203 appliances 197 applications 197 automotive 197

blowing agents 185 body forming 195 building and construction 198 butt welding 194 closed cell 173 construction 202 crosslinking agent 185 electronics 199 expanded (non-crosslinked) beads 177 extruded crosslinked 179 extruded non-crosslinked foam 174 foam density 196 foam structure 196 food contact 202 heat impression moulding 195 heat moulding 194 injection moulded process 189 manufacturing processes 174 marine 198 materials 174, 176 medical and health care 198 military 199 MuCell technology 176 nitrogen autoclave process 189 non-CFC blown 176 open cell 173 packaging 199 polymers 183 post manufacturing operations 194 press moulding 189 press moulded crosslinked 186 Pressure and temperature system 179 properties of 195 recycling processes 193 sheet lamination 194 single stage extruder 174 single stage process 187 specifications 200 sports and leisure 199

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Handbook of Polymer Foams tandem extrusion system 174 temperature 196 thermoforming 194 toys 202 two-stage process 188 vacuum forming 195 Polyols 57 copolymer 89, 90 functionality of 58 polyester 89 polyether 89, 91 Polystyrene foam 5 Polyurethane foams 94 polyols for 58 Potassium oleate soap solution formulation 210 PVC 246 plastisols 156

R Recycled expanded polystyrene slate replacement 53 wood substitute 52 Recycling compaction machines 52 consolidated granules 193 energy recovery 193 extrusion 193 granulation 193 heat moulded 193 reuse 193 solvent-based system 52 thermal system 52 Reticulated foams 111 Retrograde vitrification 261 Rigid foams isocyanate-based 55 Rigid polyurethane foams 7, 55 appliance industry 80

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applications 78 blowing agents for 65 comparative costs 69 construction 78 glycolysis 75 insulating board 59 laminated panels 74 manufacturing processes 73 properties of 76 recycling 76 recycling processes for 75 refrigerators and freezers 80 sandwich panels 79 Rigid PU foam boards thermal conductivity of 78 Rigid PVC foam 123 blowing agents 133 Celuka process 128, 130 chemical blowing agents 133 co-extrusion 130 flexural properties 145 foam density 131 foam formulation 132 foamed composites 147 formulations 141 impact behaviour 145 lubricants 141 markets 124 mechanical properties 143, 145 microcellular foam 146 physical blowing agents 137 processing aids 138 processing temperature 132 properties 143 recycled 146 recycling 145 stabilisers 140 volumetric flow rate 132

Subject Index

S

W

Sandwich boards metal faced 67 Styrene-butadiene rubber latex formulation 233 Silane crosslinking 185 Slabstock 101 mix head 100 Slabstock machines 99 Solid PVC properties of 144 Stabilisers carboxylates 140, 141 lead and zinc stearates 140 mercaptides 140 organotin 140 Sulfer formulations 210 Surfactants 72 Synthetic rubber latices 216

Wallcoverings inhibited foamed 168

Y Young’s modulus 3

T Talalay process 207, 231, 232 curing 234 gelling 234 Technical foams 111 Thermal expansion coefficient 8 Thermal insulation foam 16 Thermal properties 6, 7 melting point 7 softening point 7 thermal conductivity 6, 7 Toluene diamine 61 isomers 88

V Variable pressure foaming 90, 103 VarioCast process 75

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