Sustainability in the Process Industry: Integration and Optimization (Green Manufacturing & Systems Engineering)

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Sustainability in the Process Industry

About the Authors Jiří Klemeš, H DSC, is one of the key personalities of the world-leading Centre of Excellence in Process Integration at the University of Manchester Institute of Science and Technology in the United Kingdom. Ferenc Friedler, DSC, is a leading research figure at the University of Pannonia in Hungary. Igor Bulatov is a researcher at the Centre for Process Integration at the University of Manchester in the United Kingdom. Petar Varbanov is a senior lecturer at the Centre for Process Integration and Intensification (CPI2) at the University of Pannonia in Hungary.

Sustainability in the Process Industry Integration and Optimization Jiří Klemeš Ferenc Friedler Igor Bulatov Petar Varbanov

New York Chicago San Francisco Lisbon London Madrid Mexico City Milan New Delhi San Juan Seoul Singapore Sydney Toronto

Copyright © 2011 by The McGraw-Hill Companies, Inc. All rights reserved. Except as permitted under the United States Copyright Act of 1976, no part of this publication may be reproduced or distributed in any form or by any means, or stored in a database or retrieval system, without the prior written permission of the publisher. ISBN: 978-0-07-160555-7 MHID: 0-07-160555-X The material in this eBook also appears in the print version of this title: ISBN: 978-0-07-160554-0, MHID: 0-07-160554-1. All trademarks are trademarks of their respective owners. Rather than put a trademark symbol after every occurrence of a trademarked name, we use names in an editorial fashion only, and to the benefit of the trademark owner, with no intention of infringement of the trademark. Where such designations appear in this book, they have been printed with initial caps. McGraw-Hill eBooks are available at special quantity discounts to use as premiums and sales promotions, or for use in corporate training programs. To contact a representative please e-mail us at [email protected]. Information contained in this work has been obtained by The McGraw-Hill Companies, Inc. (“McGraw-Hill”) from sources believed to be reliable. However, neither McGraw-Hill nor its authors guarantee the accuracy or completeness of any information published herein, and neither McGraw-Hill nor its authors shall be responsible for any errors, omissions, or damages arising out of use of this information. This work is published with the understanding that McGraw-Hill and its authors are supplying information but are not attempting to render engineering or other professional services. If such services are required, the assistance of an appropriate professional should be sought. TERMS OF USE This is a copyrighted work and The McGraw-Hill Companies, Inc. (“McGrawHill”) and its licensors reserve all rights in and to the work. Use of this work is subject to these terms. Except as permitted under the Copyright Act of 1976 and the right to store and retrieve one copy of the work, you may not decompile, disassemble, reverse engineer, reproduce, modify, create derivative works based upon, transmit, distribute, disseminate, sell, publish or sublicense the work or any part of it without McGrawHill’s prior consent. You may use the work for your own noncommercial and personal use; any other use of the work is strictly prohibited. Your right to use the work may be terminated if you fail to comply with these terms. THE WORK IS PROVIDED “AS IS.” McGRAW-HILL AND ITS LICENSORS MAKE NO GUARANTEES OR WARRANTIES AS TO THE ACCURACY, ADEQUACY OR COMPLETENESS OF OR RESULTS TO BE OBTAINED FROM USING THE WORK, INCLUDING ANY INFORMATION THAT CAN BE ACCESSED THROUGH THE WORK VIA HYPERLINK OR OTHERWISE, AND EXPRESSLY DISCLAIM ANY WARRANTY, EXPRESS OR IMPLIED, INCLUDING BUT NOT LIMITED TO IMPLIED WARRANTIES OF MERCHANTABILITY OR FITNESS FOR A PARTICULAR PURPOSE. McGraw-Hill and its licensors do not warrant or guarantee that the functions contained in the work will meet your requirements or that its operation will be uninterrupted or error free. Neither McGraw-Hill nor its licensors shall be liable to you or anyone else for any inaccuracy, error or omission, regardless of cause, in the work or for any damages resulting therefrom. McGraw-Hill has no responsibility for the content of any information accessed through the work. Under no circumstances shall McGraw-Hill and/or its licensors be liable for any indirect, incidental, special, punitive, consequential or similar damages that result from the use of or inability to use the work, even if any of them has been advised of the possibility of such damages. This limitation of liability shall apply to any claim or cause whatsoever whether such claim or cause arises in contract, tort or otherwise.

Contents

1

2

3

Preface . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Acknowledgments . . . . . . . . . . . . . . . . . . . . . . . . . . . .

xv xxi

Introduction and Defi nition of the Field . . . . . . . . 1.1 Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1.2 Energy Efficiency . . . . . . . . . . . . . . . . . . . . . . . . 1.3 Screening and Scoping: Auditing, Benchmarking, and Good Housekeeping . . . 1.4 Balancing and Flowsheeting Simulation as a Basis for Optimization . . . . . . . . . . . . . . . . 1.5 Integrated Approach: Process Integration . . . 1.6 Optimal Process Synthesis and Combinatorial Graphs ................................ 1.7 How to Apply the Process Integration and Optimization Technology . . . . . . . . . . . . . . . . .

1 1 3

Process Integration . . . . . . . . . . . . . . . . . . . . . . . . . . . 2.1 Introduction: The Need for Process Integration . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2.2 What Is Process Integration? . . . . . . . . . . . . . . . 2.3 History and Development of Process Integration 2.4 Pinch Technology and Targeting Heat Recovery: The Thermodynamic Roots . . . . . . 2.5 Supertargeting: Full-Fledged HEN Targeting 2.6 Modifying the Pinch Idea for HEN Retrofit . . 2.7 Mass Exchange and Water Networks . . . . . . . 2.8 Benefits of Process Integration . . . . . . . . . . . . . 2.9 The Role of PI in Making Industry Sustainable 2.10 Examples of Applied Process Integration . . . . 2.11 Summary . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

11

Process Optimization . . . . . . . . . . . . . . . . . . . . . . . . . 3.1 Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3.2 Model Building and Optimization: General Framework and Workflow . . . . . . . . . . . . . . . .

5 7 7 8 9

11 12 12 14 15 16 17 18 20 20 22 23 23 24

v

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Contents 3.3

3.4 3.5

3.6 3.7

3.8 3.9 3.10

Optimization: Definition and Mathematical Formulation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3.3.1 What Is Optimization? . . . . . . . . . . . . . 3.3.2 Mathematical Formulation of Optimization Problems . . . . . . . . . . . . Main Classes of Optimization Problems . . . . Conditions for Optimality . . . . . . . . . . . . . . . . 3.5.1 Conditions for Local Optimality . . . . 3.5.2 Conditions for Global Optimality . . . Deterministic Algorithms for Solving Continuous Linear Optimization Problems . . . . . . . . . . . . . Deterministic Algorithms for Solving Continuous Nonlinear Optimization Problems . . . . . . . . . . 3.7.1 Search Algorithms for Nonlinear Unconstrained Problems . . . . . . . . . . . 3.7.2 Algorithms for Solving Constrained Nonlinear Problems . . . . . . . . . . . . . . . Deterministic Methods for Solving Discrete Problems . . . . . . . . . . . . . . . . . . . . . . . . Stochastic Search Methods for Solving Optimization Problems . . . . . . . . . . . . . . . . . . . Creating Models . . . . . . . . . . . . . . . . . . . . . . . . . 3.10.1 Conceptual Modeling . . . . . . . . . . . . . 3.10.2 Mathematical Modeling of Processes: Constructing the Equations . . . . . . . . 3.10.3 Choosing an Objective Function . . . . 3.10.4 Handling Process Complexity . . . . . . 3.10.5 Applying Process Insight . . . . . . . . . . 3.10.6 Handling Model Nonlinearity . . . . . . 3.10.7 Evaluating Model Adequacy and Precision . . . . . . . . . . . . . . . . . . . . . . . . .

4 Process Integration for Improving Energy Efficiency . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4.1 Introduction to Heat Exchange and Heat Recovery . . . . . . . . . . . . . . . . . . . . . . . . . . . 4.1.1 Heat Exchange Matches . . . . . . . . . . . . 4.1.2 Implementing Heat Exchange Matches . . . . . . . . . . . . . . . . . . . . . . . . . 4.2 Basics of Process Integration . . . . . . . . . . . . . . . 4.2.1 Process Integration and Heat Integration . . . . . . . . . . . . . . . . . . . . . . .

25 25 25 26 28 28 28 29 29 30 31 31 32 33 34 35 37 38 40 41 43 45 45 46 47 47 47

Contents

4.3

4.4

4.5

4.6

5

4.2.2 Hierarchy of Process Design . . . . . . . . 4.2.3 Performance Targets . . . . . . . . . . . . . . . 4.2.4 Heat Recovery Problem Identification Basic Pinch Technology . . . . . . . . . . . . . . . . . . . 4.3.1 Setting Energy Targets . . . . . . . . . . . . . 4.3.2 The Heat Recovery Pinch . . . . . . . . . . 4.3.3 Numerical Targeting: The Problem Table Algorithm . . . . . . . . . . . . . . . . . . 4.3.4 Threshold Problems . . . . . . . . . . . . . . . 4.3.5 Multiple Utilities Targeting . . . . . . . . . Extended Pinch Technology . . . . . . . . . . . . . . . 4.4.1 Heat Transfer Area, Capital Cost, and Total Cost Targeting . . . . . . . . . . . . . . . 4.4.2 Heat Integration of Energy-Intensive Processes . . . . . . . . . . . . . . . . . . . . . . . . 4.4.3 Process Modification . . . . . . . . . . . . . . HEN Synthesis . . . . . . . . . . . . . . . . . . . . . . . . . . 4.5.1 The Pinch Design Method . . . . . . . . . . 4.5.2 Superstructure Approach . . . . . . . . . . 4.5.3 A Hybrid Approach . . . . . . . . . . . . . . . 4.5.4 Key Features of the Resulting Networks . . . . . . . . . . . . . . . . . . . . . . . . Total Site Energy Integration . . . . . . . . . . . . . . 4.6.1 Total Site Data Extraction . . . . . . . . . . 4.6.2 Total Site Profiles . . . . . . . . . . . . . . . . . . 4.6.3 Heat Recovery via the Steam System . . 4.6.4 Power Cogeneration . . . . . . . . . . . . . . . 4.6.5 Advanced Total Site Optimization and Analysis . . . . . . . . . . . . . . . . . . . . . . . . .

Mass Integration . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5.1 Water Integration . . . . . . . . . . . . . . . . . . . . . . . . 5.2 Minimizing Water Use and Maximizing Water Reuse . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5.2.1 Legislation . . . . . . . . . . . . . . . . . . . . . . . 5.2.2 Best Available Techniques . . . . . . . . . . 5.2.3 Water Footprint . . . . . . . . . . . . . . . . . . . 5.2.4 Minimizing Water Usage and Wastewater . . . . . . . . . . . . . . . . . . . . . . 5.3 Introduction to Water Pinch Analysis . . . . . . . 5.4 Flow-Rate Targeting with the Material Recovery Pinch Diagram . . . . . . . . . . . . . . . . . .

47 48 48 50 51 54 56 60 61 69 69 71 80 81 81 93 95 96 96 97 97 99 101 102 105 105 106 106 107 108 111 113 116

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Contents 5.5 5.6

5.7 6

MRPD Applied to Fruit Juice Case Study . . . . Water Minimization via Mathematical Optimization . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5.6.1 Introduction to Mathematical Optimization . . . . . . . . . . . . . . . . . . . . . 5.6.2 Illustrative Example: A Brewery Plant Summary . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

117 118 118 120 122

Further Applications of Process Integration . . . . . 123 6.1 Design and Management of Hydrogen Networks . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 123 6.2 Oxygen Pinch Analysis . . . . . . . . . . . . . . . . . . . 125 6.3 Combined Analyses, I: Energy-Water, Oxygen-Water, and Pinch-Emergy . . . . . . . . . 126 6.3.1 Simultaneous Minimization of Energy and Water Use . . . . . . . . . . . . . 126 6.3.2 Oxygen-Water Pinch Analysis . . . . . . 128 6.3.3 Emergy-Pinch Analysis . . . . . . . . . . . . 130 6.4 Combined Analysis, II: Budget-Income-Time, Materials Reuse-Recycling, Supply Chains, and CO2 Emissions Targeting . . . . . . . . . . . . . . 131 6.4.1 Budget-Income-Time Pinch Analysis . 131 6.4.2 Materials Reuse-Recycle and Property Pinch Analysis . . . . . . . . . . . . . . . . . . . 133 6.4.3 Pinch Analysis of Supply Chains . . . . 136 6.4.4 Using the Pinch to Target CO2 Emissions . . . . . . . . . . . . . . . . . . . . . . . . 138 6.4.5 Regional Resource Management . . . . 139 6.5 Heat-Integrated Power Systems: Decarbonization and Low-Temperature Energy 142 6.5.1 Decarbonization . . . . . . . . . . . . . . . . . . 142 6.5.2 Low-Temperature Energy . . . . . . . . . . 143 6.6 Integrating Reliability, Availability, and Maintainability into Process Design . . . . . . . . 144 6.6.1 Integration . . . . . . . . . . . . . . . . . . . . . . . 144 6.6.2 Optimization . . . . . . . . . . . . . . . . . . . . . 146 6.7 Pressure Drop and Heat Transfer Enhancement in Process Integration . . . . . . . . . . . . . . . . . . . . 146 6.8 Locally Integrated Energy Sectors and Extended Total Sites . . . . . . . . . . . . . . . . . . . . . . 148 6.9 Summary . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 149

Contents 7

8

9

Process Optimization Frameworks . . . . . . . . . . . . . 7.1 Classic Approach: Mathematical Programming 7.2 Structural Process Optimization: P-Graphs . . 7.2.1 Process Representation via P-Graphs 7.2.2 The P-Graph’s Significance for Structural Optimization . . . . . . . . . . . 7.2.3 The P-Graph’s Mathematical Engine: MSG, SSG, and ABB . . . . . . . . . . . . . . . 7.3 Scheduling of Batch Processes: S-Graphs . . . . 7.3.1 Scheduling Frameworks: Suitability and Limitations . . . . . . . . . . . . . . . . . . . 7.3.2 S-Graph Framework for Scheduling . .

151 151 153 154

Combined Process Integration and Optimization 8.1 The Role of Optimization in Process Synthesis 8.2 Optimization Tools for Efficient Implementation of PI . . . . . . . . . . . . . . . . . . . . . 8.3 Optimal Process Synthesis . . . . . . . . . . . . . . . . 8.3.1 Reaction Network Synthesis . . . . . . . . 8.3.2 Optimal Synthesis of Heterogeneous Flowsheets . . . . . . . . . . . . . . . . . . . . . . . 8.3.3 Synthesis of Green Biorefineries . . . . . 8.3.4 Azeotropic Distillation Systems . . . . . 8.4 Optimal Synthesis of Energy Systems . . . . . . 8.4.1 Simple Heat Integration . . . . . . . . . . . . 8.4.2 Optimal Retrofit Design . . . . . . . . . . . 8.5 Optimal Scheduling for Increased Throughput, Profit, and Security . . . . . . . . . . . . . . . . . . . . . . . 8.5.1 Maximizing Throughput and Revenue 8.5.2 Heat-Integrated Production Schedules 8.6 Minimizing Emissions and Effluents . . . . . . . 8.7 Availability and Reliability . . . . . . . . . . . . . . . . 8.8 Summary . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

165 165

Software Tools . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 9.1 Overview of Available Tools . . . . . . . . . . . . . . . 9.2 Graph-Based Process Optimization Tools . . . 9.2.1 PNS Solutions . . . . . . . . . . . . . . . . . . . . 9.2.2 S-Graph Studio . . . . . . . . . . . . . . . . . . . 9.3 Heat Integration Tools . . . . . . . . . . . . . . . . . . . . 9.3.1 SPRINT . . . . . . . . . . . . . . . . . . . . . . . . . .

191 191 191 191 193 195 195

155 157 159 159 161

166 167 167 169 171 173 176 176 177 179 179 180 183 186 190

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Contents 9.3.2 HEAT-int . . . . . . . . . . . . . . . . . . . . . . . . 9.3.3 STAR . . . . . . . . . . . . . . . . . . . . . . . . . . . . 9.3.4 SITE-int . . . . . . . . . . . . . . . . . . . . . . . . . . 9.3.5 WORK . . . . . . . . . . . . . . . . . . . . . . . . . . . 9.3.6 HEXTRAN . . . . . . . . . . . . . . . . . . . . . . . 9.3.7 SuperTarget . . . . . . . . . . . . . . . . . . . . . . 9.3.8 Spreadsheet-Based Tools . . . . . . . . . . . Mass Integration Software: WATER . . . . . . . . Flowsheeting Simulation Packages . . . . . . . . . 9.5.1 ASPEN . . . . . . . . . . . . . . . . . . . . . . . . . . 9.5.2 HYSYS and UniSim Design . . . . . . . . . 9.5.3 gPROMS . . . . . . . . . . . . . . . . . . . . . . . . . 9.5.4 CHEMCAD . . . . . . . . . . . . . . . . . . . . . . 9.5.5 PRO/II . . . . . . . . . . . . . . . . . . . . . . . . . . . General-Purpose Optimization Packages . . . . 9.6.1 GAMS . . . . . . . . . . . . . . . . . . . . . . . . . . . 9.6.2 MIPSYN . . . . . . . . . . . . . . . . . . . . . . . . . 9.6.3 LINDO . . . . . . . . . . . . . . . . . . . . . . . . . . 9.6.4 Frontline Systems . . . . . . . . . . . . . . . . . 9.6.5 ILOG ODM . . . . . . . . . . . . . . . . . . . . . . Mathematical Modeling Suites . . . . . . . . . . . . . 9.7.1 MATLAB . . . . . . . . . . . . . . . . . . . . . . . . 9.7.2 Alternatives to MATLAB . . . . . . . . . . . Other Tools . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 9.8.1 Modelica . . . . . . . . . . . . . . . . . . . . . . . . . 9.8.2 Emerging Trends . . . . . . . . . . . . . . . . . . 9.8.3 Balancing and Flowsheeting Simulation for Energy-Saving Analysis . . . . . . . . . 9.8.4 Integrating Renewable Energy into Other Energy Systems . . . . . . . . . . . . .

195 195 198 198 199 200 200 201 202 202 203 204 205 206 206 206 207 208 209 209 210 210 211 211 211 212

Examples and Case Studies . . . . . . . . . . . . . . . . . . . . 10.1 Heat Pinch Technology . . . . . . . . . . . . . . . . . . . 10.1.1 Heat Pinch Technology: First Problem 10.1.2 Heat Pinch Technology: Second Problem . . . . . . . . . . . . . . . . . . . 10.2 Total Sites . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 10.2.1 Total Sites: First Problem . . . . . . . . . . . 10.2.2 Total Sites: Second Problem . . . . . . . . . 10.3 Integrated Placement of Processing Units and Data Extraction . . . . . . . . . . . . . . . . . . . . . .

219 219 219

9.4 9.5

9.6

9.7

9.8

10

215 216

224 226 226 231 234

Contents

11

12

10.4 Utility Placement . . . . . . . . . . . . . . . . . . . . . . . . 10.4.1 Utility Placement: First Problem . . . . 10.4.2 Utility Placement: Second Problem . . 10.5 Water Pinch Technology . . . . . . . . . . . . . . . . . . 10.5.1 Water Pinch Technology: First Problem 10.5.2 Water Pinch Technology: Second Problem . . . . . . . . . . . . . . . . . .

238 238 243 247 247

Industrial Applications and Case Studies . . . . . . . 11.1 Energy Recovery from an FCC Unit . . . . . . . . 11.2 De-bottlenecking a Heat-Integrated Crude-Oil Distillation System . . . . . . . . . . . . . . . . . . . . . . . 11.3 Minimizing Water and Wastewater in a Citrus Juice Plant . . . . . . . . . . . . . . . . . . . . . . . . 11.4 Efficient Energy Use in Other Food and Drink Industries . . . . . . . . . . . . . . . . . . . . . . . . . 11.5 Synthesis of Industrial Utility Systems . . . . . . 11.6 Heat and Power Integration in Buildings and Building Complexes . . . . . . . . . . . . . . . . . . . . . . 11.7 Optimal Design of a Supply Chain . . . . . . . . . 11.8 Scheduling a Large-Scale Paint Production System ................................

253 253

Typical Pitfalls and How to Avoid Them . . . . . . . . 12.1 Data Extraction . . . . . . . . . . . . . . . . . . . . . . . . . . 12.1.1 When Is a Stream a Stream? . . . . . . . . 12.1.2 How Precise Must the Data Be at Each Step? . . . . . . . . . . . . . . . . . . . . . . . 12.1.3 How Can Considerable Changes in Specific Heat Capacities Be Handled? 12.1.4 What Rules and Guidelines Must Be Followed to Extract Data Properly? . . 12.1.5 How Can the Heat Loads, Heat Capacities, and Temperatures of an Extracted Stream Be Calculated? . . . . 12.1.6 How “Soft” Are the Data in a Plant or Process Flowsheet? . . . . . . . . . . . . . . . . 12.1.7 How Can Capital Costs and Operating Costs Be Estimated? . . . . . . . . . . . . . . . 12.2 Integration of Renewables: Fluctuating Demand and Supply . . . . . . . . . . . . . . . . . . . . . 12.3 Steady-State and Dynamic Performance . . . . .

281 283 284

249

256 262 268 271 275 277 279

285 286 287

289 290 290 292 292

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Contents 12.4 Interpreting Results . . . . . . . . . . . . . . . . . . . . . . 12.5 Making It Happen . . . . . . . . . . . . . . . . . . . . . . .

293 293

13

Information Sources and Further Reading . . . . . . 13.1 General Sources of Information . . . . . . . . . . . . 13.1.1 Conferences . . . . . . . . . . . . . . . . . . . . . . 13.1.2 Journals . . . . . . . . . . . . . . . . . . . . . . . . . 13.1.3 Service Providers . . . . . . . . . . . . . . . . . 13.1.4 Projects . . . . . . . . . . . . . . . . . . . . . . . . . . 13.2 Heat Integration . . . . . . . . . . . . . . . . . . . . . . . . . 13.2.1 Conferences . . . . . . . . . . . . . . . . . . . . . . 13.2.2 Journals . . . . . . . . . . . . . . . . . . . . . . . . . 13.2.3 Service Providers . . . . . . . . . . . . . . . . . 13.2.4 Projects . . . . . . . . . . . . . . . . . . . . . . . . . . 13.3 Mass Integration . . . . . . . . . . . . . . . . . . . . . . . . . 13.3.1 Conference . . . . . . . . . . . . . . . . . . . . . . . 13.3.2 Journals . . . . . . . . . . . . . . . . . . . . . . . . . 13.3.3 Service Providers . . . . . . . . . . . . . . . . . 13.3.4 Projects . . . . . . . . . . . . . . . . . . . . . . . . . . 13.4 Combined Analysis . . . . . . . . . . . . . . . . . . . . . . 13.4.1 Conferences . . . . . . . . . . . . . . . . . . . . . . 13.4.2 Journals . . . . . . . . . . . . . . . . . . . . . . . . . 13.4.3 Service Providers . . . . . . . . . . . . . . . . . 13.4.4 Projects . . . . . . . . . . . . . . . . . . . . . . . . . . 13.5 Optimization for Sustainable Industry . . . . . . 13.5.1 Conferences . . . . . . . . . . . . . . . . . . . . . . 13.5.2 Journals . . . . . . . . . . . . . . . . . . . . . . . . . 13.5.3 Service Providers . . . . . . . . . . . . . . . . . 13.5.4 Projects . . . . . . . . . . . . . . . . . . . . . . . . . .

295 295 295 297 297 301 301 301 301 301 303 304 304 304 305 306 306 306 307 307 308 309 309 310 310 311

14

Conclusions and Further Information . . . . . . . . . . 14.1 Further Reading . . . . . . . . . . . . . . . . . . . . . . . . . 14.1.1 Books and Key Articles . . . . . . . . . . . . 14.1.2 Lecture Notes and Online Teaching Resources . . . . . . . . . . . . . . . . . . . . . . . . 14.2 Development Trends . . . . . . . . . . . . . . . . . . . . . 14.2.1 Top-Level Analysis . . . . . . . . . . . . . . . . 14.2.2 Maintenance Scheduling, Maintainability, and Reliability . . . . . 14.2.3 Hybrid Energy Conversion Systems . . . 14.2.4 Integration of Renewables and Waste

313 313 313 315 316 316 316 317 317

Contents 14.2.5 Better Utilization of Low-Grade Heat 14.2.6 Energy Planning That Accounts for Carbon Footprint . . . . . . . . . . . . . . . . . 14.3 Conclusions . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

319 320

Bibliography

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321

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345

Index

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Preface

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his book describes and analyzes an amalgamation of two effective ways to considerably improve the efficiency and sustainability of processing industries: Process Integration and optimization. It is the result of collaborative efforts by two groups: researchers at the Centre for Process Integration, the University of Manchester, UK (a renowned center of excellence in this field), and the Faculty of Information Technology at the University of Pannonia, Hungary, as represented by the Centre for Process Integration and Intensification (CPI2) and the Centre for Advanced Process Optimization. The University of Pannonia centers are highly regarded for their achievements in optimization, and the P-graph and S-graph approaches to process optimization originated at this university. The book should provide support for graduate and postgraduate students worldwide as well as for Continuing Professional Development (CPD) courses and for practitioners from various fields of the processing industry. Its chapters analyze a number of problems of practical significance and also suggest various options for solving them to the benefit of modern society. The book provides a wealth of material for postgraduate teaching and further professional training. It is supported by the expertise stemming from the authors’ work as well as by a pool of case studies of varying complexity that have been collected over the years. This wide-ranging material presented here has been selected and refined over years of postgraduate teaching, further CPD courses, and training for the industry. It includes eight industry-based demonstration case studies and nine testing examples with the solutions developed. An unbiased evaluation and overview of the software tools available for learning, teaching, and industrial applications are also included. Text discussions are complemented by many figures to clarify details and enhance understanding. The book contains 14 chapters and a comprehensive bibliography. Chapter 1 is devoted to introducing and defining the field, and it also includes a basic assessment of energy efficiency. It starts with screening and scoping, which include auditing, benchmarking, and recommendations for good housekeeping. Next it describes an

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Preface important tool: balancing and flowsheeting simulation as a basis for optimization. It is on this basis that an integrated approach to optimization, Process Integration, is introduced. This approach is then connected to optimal process synthesis and combinatorial graphs. The important question of how to apply the Process Integration and Optimization Technology arises and is dealt with. This is further tackled and analyzed in the following chapters. Chapter 2 deals with the basic outline and definitions of Process Integration (PI). It begins with a historical and methodological introduction, briefly reviewing refinements and extensions of PI over its years of development. The thermodynamic roots of the Pinch Technology and of targeting heat recovery are introduced, followed by one of the key graphical constructions in the PI methodology: Composite Curves (CCs) for targeting process heat recovery. Supertargeting, or targeting for a full-fledged Heat Exchanger Network (HEN), is the next logical step. These tools are used to assess modifications of the Pinch idea for HEN retrofitting. Although PI was initially based on Heat Integration, an important spin-off was the development of integration for mass exchange and water networks. The chapter concludes with remarks on the role of PI in making industry sustainable. Chapter 3 introduces the other key methodology used for sustainable process design and synthesis: optimization. It presents a general framework and workflow of model building and follow-up optimization, including models that incorporate “black boxes” or “gray boxes.” It is critical to understand both the meaning and the mathematical formulation of optimization. Toward this end, the following questions are answered: What is optimization? What are the main classes of optimization problems? How are optimization problems formulated mathematically? What are the conditions for local or global optimality? This is followed by introducing deterministic algorithms for solving continuous linear and nonlinear, constrained and unconstrained, optimization problems. The most popular optimization methods and algorithms that employ stochastic search are also reviewed. The middle part of Chapter 3 is devoted to model creation. It includes a detailed description of conceptual modeling: extracting data about the operating units, identifying network and topology data, constructing equations to represent the processes, and finally choosing a right objective function. The last part of this chapter discusses how to handle complexity and nonlinearity as well as how to apply process insight when evaluating model adequacy and precision. Chapter 4 covers the core topic from which the development of PI began: improving the energy efficiency of individual processes and the PI extension into Total Sites. The chapter starts by introducing heat exchange, heat recovery, and heat exchange matches so that readers will be prepared for the remaining chapter content. The

Preface strategic view of Process Integration is outlined; this includes an overview of the hierarchy of process design, the meaning of performance targets, and the practical issue of identifying heat recovery problems from process flowsheets. These three topics are closely interrelated. Without properly applying the process design hierarchy, the performance targets cannot find a practical application and use. However, the process design hierarchy would be difficult to apply without employing performance targets and estimating upper bounds on process performance or lower bounds on total cost. Meaningful and practically useful heat-integrated designs cannot be obtained without appropriate identification of the heat recovery problem, a process referred to as data extraction. The chapter proceeds to describe the use of Composite Curves to set heat recovery targets, the Problem Table Algorithm for numerical targeting, and the Heat Recovery Pinch. These tools and concepts form the basis of Pinch Technology, defining the thermodynamic capabilities of the heat recovery problems. The more advanced aspects are discussed next; these include threshold problems, targeting multiple utilities via the Grand Composite Curve, and establishing targets for heat transfer area, capital cost, and total cost. There is a short overview of options for modifying the core process (which defines the heat recovery problem) that highlights the usefulness of Pinch Technology and targeting for improving its energy efficiency. The chapter then focuses on the synthesis of Heat Exchanger Networks; the approach mainly follows the Pinch Design Method, but there is discussion of the superstructure-based and hybrid methods used for HEN synthesis. The next step is Total Site Integration, which provides the necessary knowledge for energy recovery over complete industrial complexes and sites. Chapter 5 deals with an extension of PI known as Mass Integration, the most widely used instance of which is Water Integration (WI). The chapter begins with a description of the methodology and bases for minimizing water use and maximizing water reuse, and the importance of legislatively imposed constraints is discussed. Best available techniques are analyzed and recommended for usage, and the concept of a water footprint is described. At this point, the stage is set for the main task: minimizing freshwater usage and wastewater effluents. For this, the methodology of Water Pinch Analysis is introduced. Also described is a related Mass Integration and targeting technique, the material recovery Pinch diagram. The chapter concludes with water minimization using the mathematical optimization approach. Both the WI and the mathematical approaches to optimization are illustrated with case studies. Chapter 6 addresses further PI opportunities that have arisen as the methodology was developed. These include: Hydrogen Networks Design and Management; Oxygen Pinch Analysis; combined analyses (energy-water, oxygen-water, Pinch-emergy, budget-income-time,

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Preface materials reuse-recycling); supply chains; CO2 emissions targeting; regional resource management; heat-integrated power systems with decarbonization and low-temperature energy systems; and the integration of reliability, availability, and maintainability with process design. An example is given of a real-life PI problem involving pressure-drop considerations during heat transfer enhancement. Several recent applications are mentioned, including a Locally Integrated Energy Sector and extended Total Sites with multiple energy carriers. Chapter 7 presents an overview of process optimization from the perspectives of Mathematical Programming (MPR) and the P-graph. The main features of these frameworks are analyzed, and it is shown that the P-graph is better suited than MPR for solving combinatorial optimization problems and, in particular, problems involving the synthesis of process networks. Optimization of process scheduling is the next topic. The most popular models and representations of process schedules are analyzed, and an efficient tool for obtaining them is introduced: the S-graph. Chapter 8 presents an integrated view of PI and optimization. It discusses how to efficiently apply them jointly in process synthesis and how to combine them. The chapter presents a number of examples of the P-graph and S-graph frameworks applied to combinations of PI and optimization. These applications are grouped thematically: (1) optimal process synthesis, including examples on reaction networks, green biorefineries, and azeotropic distillation; (2) synthesis of general energy systems involving Heat Integration and optimal retrofit; (3) optimal scheduling for maximizing throughput and revenue; (4) minimizing emissions via optimal synthesis of advanced energy conversion systems using Fuel-Cell Combined Cycles; and (5) availability and reliability features. Chapter 9 reviews the software tools for process modeling, integration, and optimization. The engineering field of sustainable design is complex in terms of scales and relationships, which makes information technology and computer software essential for solving problems—preferably with a user-friendly interface. The chapter reviews a wide spectrum of tools, as follows: (1) graph-based process optimization (process network synthesis solutions implementing P-graphs and the S-Graph Studio software); (2) Energy and Mass Integration tools designed to optimize the implementation of Heat Integration (SPRINT, HEAT-int, HEXTRAN, SuperTarget, spreadsheetbased tools), Total Site Integration (STAR, SITE-int), power generation and combined heat and power (STAR, WORK), and water systems integration (WATER); (3) process flowsheeting and simulation packages developed or supported by the major players (Aspen Plus, HYSYS and UniSim, gPROMS, CHEMCAD, PRO/II); (4) generalpurpose optimization systems (GAMS, MIPSYN); (5) computer algebra systems; and (6) other tools.

Preface Chapter 10 is a collection of examples and case studies that support the material presented in previous chapters. This selection of problems was collected by the authors over decades of teaching and consulting. Most of the problems have step-by-step solutions that feature comments and guidance for mastering the methodology. The examples are organized in several thematic groups: basic Heat Integration, Total Sites, integrated placement of energy-intensive processes, placing utilities, and Water Pinch Technology. Chapter 11 contains advanced examples that are based on industrial case studies, most of which were performed and published by the authors. The case studies presented include: (1) retrofit of a fluid catalytic cracking unit process that featured a large-scale heat recovery network; (2) de-bottlenecking of a heat-integrated crude-oil distillation process; (3) water system optimization of a citrus juice plant; (4) efficient water use in other food industries; (5) synthesis of industrial utility systems; (6) heat and power integration in buildings and building complexes; (6) optimal supply chain design; and (7) scheduling a large-scale paint production system. Chapter 12 distills some important and rare expertise: typical pitfalls and how to avoid them. It addresses possible (and probable) difficulties encountered during problem formulation and data extraction. The chapter raises seemingly trivial yet fundamental questions: When is a stream a stream? How precise must the data be at each step? How can extreme changes in specific heat capacity be handled? What rules and guidelines must be followed to properly extract data? How can the heat loads, heat capacities, and temperatures of an extracted stream be calculated? How “soft” are the data in a plant or process flowsheet? How can capital costs and operating costs be estimated? The provided answers are based on long-term experience and could help readers to solve the right problem—that is, a problem that accurately reflects the reality of the process under consideration. The chapter also addresses the integration of renewables that exhibit fluctuating demand and supply rates as well as steady-state and dynamic performance considerations. The chapter concludes with recommendations for interpreting results and suggestions on the successful advocacy and implementation of sustainable and optimal design. Chapter 13 consists solely of information on sources for further reading and information gathering. The various sources of information about optimization and integration in the process industry are arranged as follows: (1) general sources of information, (2) Heat Integration, (3) Mass Integration, (4) combined analysis, and (5) optimization for sustainable industry. Each topic is subdivided into sections on conferences, journals, service providers, and projects. Chapter 14 presents conclusions and sources of further information. Suggestions for further reading point to books and

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Preface lecture notes containing applications and details that could not be adequately described in a book of this size. The book ends with a comprehensive bibliography that provides details of works cited in the text and serves also as a source of information and directions for further study. This book is intended to increase awareness of the principal methodologies that could contribute to improving energy and water efficiency in processing plants while reducing their environmental impact. Many additional illustrative examples could well have been discussed, but space limitations required that the authors select the most important features from a variety of fields and processing industries; even so, hundreds of references are included for seekers of more information. If the authors have managed to raise the interest and awareness of readers, then this book has fulfilled its intentions. Jiří Klemeš Ferenc Friedler Igor Bulatov Petar Varbanov

Acknowledgments

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e acknowledge the support from the European Community–funded project entitled “Integrated Waste to Energy Management to Prevent Global Warming,” or INEMAGLOW. We would like to thank Prof. Robin Smith and Mr. Simon Perry from the University of Manchester for numerous discussions about the finer points of PI and optimization methodology. We also acknowledge with much gratitude the input of all collaborators who contributed to this book. Their dedication, timely responses, and willingness to accept editorial comments and suggestions are greatly appreciated. We received invaluable help from the staff of the Faculty of Information Technology at the University of Pannonia in Hungary: Dr. Rozália Pigler-Lakner, Dr. István Heckl, Dr. Boton Bertók, Dr. Zoltán Süle, Mr. Máté Hegyháti, and Ms. Adrienn Sas. Substantial contributions were also made by Hon Loong Lam—林汉龙 and Zsófia Fodor, Ph.D. students at CPI2. Special thanks go to colleagues and close collaborators worldwide who shared their latest methodologies and case studies. It would be impossible to list all those involved, but we should like to mention a few: Prof. L. T. Fan, Department of Chemical Engineering, Kansas State University, Manhattan, Kansas, USA; Dr. Dominic C. Y. Foo, Department of Chemical and Environmental Engineering, University of Nottingham, Malaysia Campus; Prof. Zdravko Kravanja, Faculty of Chemistry and Chemical Engineering, University of Maribor, Slovenia; Prof. Valentin Ples¸u, Centre for Technology Transfer for the Process Industries, Department of Chemical Engineering, University POLITEHNICA, Bucharest; and Prof. Petr Stehlík, Brno University of Technology, Institute of Process and Environmental Engineering, UPEI VUT Brno, the Czech Republic. The authors appreciate the editing and production efforts of the following people: Taisuke Soda, Michael Penn, Stephen Smith, Richard Ruzycka, and Michael Mulcahy of McGraw-Hill, and Aloysius Raj and the staff at Newgen. It has been a great pleasure for us to work with all of you.

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CHAPTER

1

Introduction and Definition of the Field 1.1

Introduction In recent years there has been increased interest in the development of renewable, non-carbon-based energy sources in order to combat the increasing threat of carbon dioxide (CO2) emissions and subsequent climatic change. More recently, the fluctuations and often large increases in the prices of oil and gas have further increased interest in employing alternative, lower-carbon or non-carbon-based energy sources. These cost and environmental concerns have led to increases in the industrial sector’s efficiency of energy use, although the use of renewable energy sources in major industry has been sporadic at best. In contrast, domestic energy supply has moved more positively toward the integration of renewable energy sources; this movement includes solar heating, heat pumps, and wind turbines. However, there have been only limited and ad hoc attempts to design a combined energy system that includes both industrial and residential buildings, and few systematic design techniques have been marshaled toward the end of producing a symbiotic system. This book provides an overview of the Process Integration and optimization methodologies and its application to improving the energy efficiency of not only industrial but also nonindustrial energy users. An additional aim is to evaluate how these methodologies can be adapted to include the integration of waste and renewable energy sources. Industrial production requires a considerable and continuous supply of energy delivered from natural resources—principally in the form of fossil fuels such as coal, oil, and natural gas. The increase in our planet’s human population and its growing nutritional

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Chapter One demands have resulted in annual increases in energy consumption. Furthermore, many nations have accelerated their development in the last 10 years, and countries (such as China and India) with large populations have seen significant increases in energy demands. This growing energy consumption has also resulted in unsteady climatic and environmental conditions in many areas because of increased emissions of CO2, NOx, SOx, dust, black carbon, and combustion process waste (Klemeš et al., 2005a; Klemeš, Bulatov, and Cockeril, 2007). It has become increasingly important to ensure that the production and processing industries take advantage of recent developments in energy efficiency and in the use of nontraditional energy sources (Houdková et al., 2008; Lam, Varbanov, and Klemeš, 2010). The additional cost is related to the amount of emitted CO2 and often takes the form of a centrally imposed tax. A workable solution to this problem would be to reduce emissions and effluents by optimizing energy consumption, increasing the efficiency of materials processing, and also increasing the efficiency of energy conversion and consumption (Klemeš et al., 2005b). Although major industry requires large supplies of energy to meet production, it is not the only sector of the world economy that is increasing its demands for energy. The particular characteristics of the other sectors (e.g., transport, residential) make optimizing for energy efficiency and cost reduction more difficult than in traditional processing industries, such as oil refining, where continuous mass production concentrated in a few locations offers an obvious potential for large energy savings (Al-Riyami, Klemeš, and Perry, 2001). In contrast, for example, agricultural production and food processing are distributed over large areas, and these activities are not continuous but rather structured in seasonal campaigns. Hence, energy demands in this sector are related to specific and limited time periods, so the design of efficient energy systems to meet this demand is more problematic than in traditional, steady-state industries. This chapter proceeds by first outlining the field of energy efficiency, including its scope, actors, and main features. The next step is to describe energy-saving techniques generally and then to specify an integrated approach: Heat Integration. An increasingly prominent issue is assessing and minimizing emissions and the carbon footprint. The carbon footprint (CFP) is defined by the U.K. Parliamentary Office for Science and Technology as the total amount of CO2 and the other greenhouse gases emitted over the full life cycle of a process or product (POST, 2006). There have been numerous studies (see, e.g., Albrecht, 2007; Fiaschi and Carta, 2007) that emphasize the “carbon neutrality” of renewable sources of energy. However, even renewable energy sources make some contribution to the overall carbon footprint, and assessment studies frequently do not account for this. The carbon footprint should also be incorporated

Introduction and Definition of the Field into any product’s life-cycle assessment (LCA); see, for example, Masruroh, Li, and Klemeš (2006).

1.2 Energy Efficiency The task of saving energy—especially at a time of rising energy costs, demand, and carbon emissions—must be taken seriously by all communities and industries. Society is driven by the economics of individual situations, and no section of society worldwide can be expected to save energy at any cost. Thus, energy-saving measures must be considered within the context of such issues as environmental factors, legislatively imposed constraints, and pressure from conscientious consumers. The simplest and most obvious technique involves energy auditing and applying good housekeeping measures. In many cases even these simple measures are not fully understood or completed in sufficient detail. To undertake a worthwhile energy audit, correct measurements are necessary. Also, because in many cases energy demand is not constant and instead fluctuates considerably, the monitoring of energy consumption has to be performed over specific (or extended) periods of time. Recommended monitoring techniques are described by various sources: utility companies, such as SEMPRA ENERGY (2009); governmental agencies, such as the U.S. Department of Housing and Urban Development (2009); and international groups, such as the International Energy Agency (Mandil, 2005). Improvements in energy efficiency must often be achieved by more complex means, such as those associated with improved design and operation. It is of paramount importance that all energy-related processes operate with maximum efficiency and minimum energy input. These systems should also ensure that they are fueled as much as possible by low-value inputs or recycled wastes, such as process outputs—for example, “off-gases” and hotwater waste (AEA Technology, 2000). To ensure that systems are designed to be as efficient as best practice allows, optimization methods are frequently employed for grassroots design, retrofit, control, and intelligent support systems for processes, plants, and buildings. One technology that has a strong reputation for improving energy efficiency through better design is Pinch Technology (Linnhoff and Vredeveld, 1984), which has been in use for more than 20 years. This technology, through feedback from practical applications and industry professionals, has been continuously developed and expanded (Klemeš et al., 1997; Smith, 2005; Klemeš, Smith, and Kim, 2008). Details on the successful applications of Pinch Technology in various industrial sectors are described in Chapter 11. The sustainability of energy systems can also be considerably improved by making use of renewable energy sources (e.g., biofuels,

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Chapter One wind, water power), which significantly reduce the generation of greenhouse gases. Implementing Combined Heat and Power (CHP) systems (AEA Technology, 2000), rather than a separate power system and heat system, can also substantially improve the efficiency of energy supply. In addition, the overall situation can be improved by certain fast-advancing technologies: heat pumps, compact heat exchangers, fuel cells (FCs), and intensified technologies. Some of these approaches are not yet fully commercialized but are gradually becoming available. Some examples discussed in AEA Technology (2000) are as follows: • Advanced gas turbines for both utility and industrial applications, including cogeneration (CHP). • Fuel cells are electrochemical devices that may be fueled by hydrogen, methane, or other organic fuels. High-temperature FCs (MCFC and SOFC) can also use cleaned and conditioned synthesis gas directly. These systems produce high-grade heat (above 500ºC) in addition to electrical power, and they are well suited to cogeneration. It is estimated that FCs typically emit 25 percent less CO2 than a gas turbine. Yet further advances are required before their full application becomes economically practical. One option is to integrate CHP and FCs (Varbanov et al., 2006). • Dividing-wall distillation technology (Triantafyllou and Smith, 1992; Hernández and Jiménez, 1999). This technology involves the separation of three components (or groups of components) in a mixture. In the past this would have required two distillation columns, with heating and cooling provided for each column. The dividing-wall technology combines the separation process into a single vessel to yield energy savings of about 30 percent and capital savings of about 25 percent (MW Kellogg, 1998). • Compact heat exchangers are generally made of thin metallic plates rather than tubes. The plates form complex and small flow passages that result in a large surface area for heat transfer per unit volume. Multistream versions of these exchangers can incorporate 12 or more streams. Compact heat exchangers can yield energy savings and also reduce the costs of capital and installation. In a case study at a U.K. refinery, potential capital savings ranged from 69 to 84 percent (EEO, 1993). Cogeneration is being increasingly applied in most sectors. For example, many oil refineries satisfy a large portion of their power demands by on-site generation, with the balance being supplied by externally purchased electricity. Usually all or almost all heating

Introduction and Definition of the Field needs are met by on-site generation of heat carriers (hot oil, steam, flue gases). CHP generation and even “tri-generation” (simultaneous production of heat, power, and cooling) offer an opportunity to reduce greenhouse gas emissions from the combined power grid– refinery system by utilizing fuel heat content more completely than do most existing power generation technologies. The improved utilization rate is achieved by recovering the heat left in the exhaust streams of the various power generating facilities (gas turbines, FCs).

1.3 Screening and Scoping: Auditing, Benchmarking, and Good Housekeeping Over the years, screening and scoping tools have had a considerable effect on reducing the costs of energy and of treating effluents, thereby improving plant profit margins. For example, energy audits performed on various food and drink processes have resulted in cost savings of 15–30 percent and in attractive returns on investment (NRCan, 2007; U.S. DOE, 2007). Because profit margins are generally small in this sector, efficient management of energy is crucial for increasing profits while simultaneously reducing the production plants’ environmental impacts. The Carbon Trust (2009) has suggested the following steps for reducing energy consumption and thus improving energy efficiency. An analogous approach can be used for optimizing the use of water and wastewater: • Good housekeeping: (1) improving staff attitude and awareness; (2) locating heat leakages; (3) preventive maintenance; (4) insulation; (5) justifying use of heating, cooling, and lighting; (6) prevention or reduction of fouling; and (7) monitoring and control. • Energy audits: (1) examining records of energy cost and consumption; (2) producing an “energy balance sheet”; (3) providing high-quality data on energy consumption and costs; (4) collecting and processing data regularly (recommended for the analysis and review of energy information); and (5) establishing a benchmark of energy consumption based on other organizations or accepted standards. • Energy Efficiency Environmental Management System, ISO 14001: (1) the management system is a network of interrelated elements; (2) these elements include responsibilities, authorities, relationships, functions, processes, procedures, practices, and resources; (3) the management system

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Chapter One establishes policies and objectives and also develops ways of applying the policies to achieve the objectives. • Responsible use of energy: in (1) energy procurement, (2) metering and billing, (3) performance measurement, (4) policy development, (5) assigning energy management responsibility, (6) energy surveying and auditing, (7) training and education, and (8) capital project management. The steps listed here have been found by the U.K. Energy Efficiency Best Practice Programme (EEBPp, 2002) to be central to any resource and waste management program. Energy screening and scoping audits fall into three main categories whose use (either individually or in combination) is based on the required depth of the study, the process to be analyzed, and the plant size: (1) the walk-through audit, which provides a quick snapshot of certain opportunities; (2) the detailed audit, which conducts an in-depth analysis of specific components; and (3) the Process Integration audit, which analyzes the plant as a whole and takes a systematic look at all processing steps and their interconnections. Audits may be performed by plant personnel, by external experts, or by teams with members from both groups. Although there are many possible options and levels of detail, typical activities include the following (NRCan, 2007): 1. Determination of the production “base case” and the reference period. 2. Collection of energy total consumption and cost (information usually available from fuel records, electricity invoices, etc.). 3. Development of a process flow chart that shows materials, energy inputs, and energy outputs for the main processing steps. 4. For the largest consumers, collection of energy data from the plant metering devices, control systems, and process flow diagrams (if current operating conditions are close to design data). In terms of the time required for (and other costs of) identifying opportunities to save energy, one efficient approach is the top-level analysis (Varbanov et al., 2004). This procedure accounts for investment limits or allowances and identifies economically justifiable energysaving opportunities, listing them in the order of their expected economic return. Measurements can be performed using portable instruments (flow rate, temperature, humidity, etc.) to determine the overall plant production of steam, refrigeration, compressed air, and hot water. Interviews with key personnel and operators can also provide valuable information about plant operations.

Introduction and Definition of the Field

1.4 Balancing and Flowsheeting Simulation as a Basis for Optimization Balancing reconciliation and flowsheeting simulation tools are frequently used for sustainability design and savings analysis; in fact, they have become the main tools in a process engineer’s toolbox. These tools help engineers to develop complete material and energy models based on measurements and/or design values and mathematical models. Consequently, these simulation tools play an important role in the technical and economic decision-making activities related to the planning and/or design stage of processes under development and to the operation of existing equipment. A number of computer-based systems have been developed to help process engineers calculate energy and mass balances. However, ongoing development costs have left only a few of these systems on the market: those whose positions have been secured by a substantial number of sales. An early overview of flowsheeting simulation was presented by Klemeš (1977). The balancing, data validation, and reconciliation technology involves a set of procedures incorporated into a software tool. Process data reconciliation has become the main method for monitoring and optimizing industrial processes as well as for component diagnosis, condition-based maintenance, and online calibration of instrumentation. According to Heyen and Kalitventzeff (2007), the main goals of this technology are: (1) to detect and correct deviations and errors of measured data so that they satisfy all balance constraints; (2) to use knowledge about the process system and structure along with measured data to compute unmeasured data wherever possible, especially key performance indicators (KPIs); and (3) to determine the postprocessing accuracy of measured and unmeasured data, including KPIs. More information about available software tools is provided in Chapter 9.

1.5

Integrated Approach: Process Integration Heat Integration is the first part of Process Integration, which provides the design foundation for CHP systems, refrigeration, air conditioning, and heat-pump systems. Process Integration is equally applicable to small, medium, and large industrial sites (e.g., power stations and oil refineries engaged in the production of petrochemicals). The technology answers one of the major challenges in the design of heating and cooling systems—namely, the complexity of energy and power integration—via a mapping strategy based on thermodynamically derived upper bounds on the system’s thermal and power performance. The efficient use of available heating and cooling resources for serving complex systems of various sizes and designations can significantly reduce energy consumption and emissions. This methodology can also be used to integrate renewable

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Chapter One energy sources such as biomass, solar photovoltaic (PV), and solar thermal into the combined heating and cooling cycles. Since 1995, the energy consumption of European Community (EC) member countries has risen by 11 percent to the equivalent of 1637 Mt (megatons) of oil equivalent (Eurostat, 2007). This increase in energy consumption contrasts with the trend of the EC population, which is growing at only about 0.4 percent annually (Eurostat, 2007). The overall share of total energy consumption by industry is declining in most countries. However, domestic energy consumption is rising. In the United Kingdom, for example, residential consumption rose from 35.6 Mt (oil equivalent) in 1971 to 48.5 Mt in 2001—an increase of 36 percent— despite increases in energy efficiency (DTI, 2006). Process Integration Technology (Pinch Technology) has been extensively used in the processing and power generating industry for more than 30 years. It was pioneered by the Department of Process Integration, UMIST (now the Centre for Process Integration, CEAS, the University of Manchester), in the late 1980s and 1990s. Heat Integration is introduced in Chapter 2 and is described in more detail in Chapter 4. Water and mass integration is covered in Chapter 5, and recent developments in the field are reviewed in Chapter 6.

1.6

Optimal Process Synthesis and Combinatorial Graphs Process synthesis is a complex engineering activity that involves process modeling (e.g., chemical engineering) as well as combinatorial challenges. Although the basic process modeling has reached a considerable level of maturity, the combinatorial aspects of the engineering problem still leave significant room for improvement. One innovative approach to process synthesis is to exploit the combinatorial nature of network optimization. This approach is used by the process-graph (P-graph) framework, which explicitly defines sets of process materials and operations and then uses efficient combinatorial algorithms to build a rigorous network superstructure that can be reduced to the optimal network topology. This is different from the Mathematical Programming (MPR) approach, where the combinatorial aspects are modeled by algebraic equations and the structural features are blended with the underlying process models. These approaches are covered in Chapters 3, 7, and 8. The P-graph framework has been successfully applied to and demonstrated on several cases of energy system design. For example, Varbanov and Friedler (2008) explored FC-based systems in a case study that evaluated energy conversion systems to reduce CO2 emissions via Fuel-Cell Combined Cycle (FCCC) subsystems that utilize biomass and/or fossil fuels. The combinatorial complexity of the problem is efficiently handled by using P-graph framework and

Introduction and Definition of the Field algorithms. The authors developed a methodology for synthesizing cost-optimal FCCC configurations that accounts for the system carbon footprint. Their results show that the high energy efficiency of such systems when using renewable fuels makes them economically viable for a wide range of conditions. This study and other case studies (and guided applications) are provided in Chapters 10 and 11.

1.7

How to Apply the Process Integration and Optimization Technology The crucial topic of applications is addressed in Chapter 12, and Chapters 13 and 14 discuss sources of further information for those who would like to learn more or who seek qualified help from leading researchers and providers worldwide. Although every effort has been made to ensure that the provided information is as comprehensive as possible, it cannot be fully exhaustive. The field of Process Integration and optimization is developing rapidly, and every month brings important advancements. For this reason, the reader is strongly encouraged to remain up-to-date by reading about and exploring new developments.

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Process Integration 2.1

Introduction: The Need for Process Integration Energy and water saving, global warming, and greenhouse gas emissions have become major technological, societal, and political issues. These issues are of strategic importance because they are all closely related to energy supply. Numerous studies have been performed on the subject of improving energy efficiency while reducing emissions of greenhouse gases, volatile organic compounds, and other pollutants. In response to these industrial and societal requirements, several novel methodologies emerged since 1970. They included process system engineering (Sargent, 1979; Sargent, 1983) and “Process Integration” (Linnhoff et al., 1982; Linnhoff et al., 1994) followed by a number of works from the UMIST Group. Both disciplines were involved in dedicated conferences such as ESCAPE (European Symposium on Computer Aided Process Engineering), which was facilitated by the European Federation of Chemical Engineering Working Party on Computer Aided Process Engineering (CAPE, 2009), and PRES (Conference on Process Integration, Modelling and Optimisation for Energy Saving and Pollution Reduction; PRES, 2009), which is supported on an annual basis by chemical and chemical engineering societies (e.g., Hungarian Chemical Society, Czech Society of Chemical Engineering, Italian Association of Chemical Engineering, Canadian Society for Chemical Engineering). It has gradually become evident that resource inputs and effluents of industrial processes are often connected to each other. Examples of this connection include the following: 1. Reducing external heating utility is usually accompanied by an equivalent reduction in the cooling utility demand (Linnhoff and Flower, 1978; Linnhoff et al., 1982; Linnhoff et al., 1994); obviously, this also tends to reduce the CO2 emissions from the corresponding sites. 2. Reducing wastewater effluents usually leads to reduced freshwater intake (Wang and Smith, 1994; Bagajewicz, 2000; Thevendiraraj et al., 2003).

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Chapter Two Reducing the consumption of resources is typically achieved by increasing internal recycling and reuse of energy and material streams instead of fresh resources and utilities. Projects for improving process resource efficiencies can offer economic benefits and also improve public perceptions of the company undertaking them. However, motivating, launching, and carrying out such projects requires proper optimization studies that are based on adequate models of the process plants.

2.2

What Is Process Integration? Process Integration (PI) is a family of methodologies for combining several processes to reduce consumption of resources and/or to reduce harmful emissions. It started as mainly Heat Integration (HI), stimulated by the energy crisis of the 1970s (Hohmann, 1971; Linnhoff and Flower, 1978; Linnhoff, Mason, and Wardle, 1979; Linnhoff et al., 1982; Linnhoff and Hindmarsh, 1983; Linnhoff and Vredeveld, 1984). This energy-saving methodology has been used extensively in the processing and power generating industry over the last 30 years. Heat Inetegration examines the potential for improving and optimizing the heat exchange between heat sources and heat sinks in order to reduce the amount of external heating and cooling required, thereby reducing costs and emissions. A systematic, rule-based design procedure has been developed that yields the maximum energy-saving design for a given system. There are several definitions of HI (using Pinch Technology); most refer to the thermal combination of steady-state process streams or batch operations for achieving heat recovery via heat exchange. More broadly, the definition of PI, as adopted by the International Energy Agency (Gundersen, 2000) is as follows: systematic and general methods for designing integrated production systems ranging from individual processes to total sites and with special emphasis on the efficient use of energy and reducing environmental effects.

2.3 History and Development of Process Integration It is remarkable that PI continues to interest researchers even 35 years after its emergence. The HI, which developed as the first part of PI, deals with the integration of heat in Heat Exchanger Networks (HENs). This methodology has been shown to have considerable application potential for complete chemical processing sites, reducing overall energy demand and emissions across the site and thus leading to a more effective and efficient site utility system. The PI and its subset HI method have also been successfully applied to the cogeneration of heat and shaft power. Further details are available elsewhere

Process Integration (Linnhoff et al., 1982; Linnhoff et al., 1994; Shenoy, 1995; Smith, 2005; El-Halwagi, 2006; Kemp 2007; Klemeš, Smith, and Kim, 2008). One of the first works in this field was Hohmann’s (1971) PhD thesis, which introduced a systematic thermodynamics-based reasoning for evaluating the minimum energy requirements for a given HEN synthesis problem. In the late 1970s this work was continued by Linnhoff and Flower, who used Hohmann’s foundation to develop the basis of Pinch Technology—now considered the cornerstone of HI. As is often the case with a pioneering innovation, this work was difficult to publish. Yet the authors’ strong commitment eventually led to the publication of their ideas in Linnhoff and Flower (1978), which has since become the most cited paper in the history of chemical engineering. Similar work (Umeda et al., 1978; Umeda, Harada, and Shiroko, 1979) was independently published in Japan, but it was Linnhoff (supported by teams from UMIST and later Linnhoff March Ltd.) who pushed the new concept through academia and industry. The publication of the first “red” book by Linnhoff et al. (1982) played a key role in the dissemination of HI methodology. This user’s guide to Pinch Analysis detailed the most common process network design problems, including HEN synthesis, heat recovery targeting, and selecting multiple utilities. These methodologies were developed and pioneered by the Department of Process Integration, UMIST (now the Centre for Process Integration, CEAS, the University of Manchester) in the late 1980s and 1990s (Linnhoff et al., 1982; Linnhoff and Vredeveld, 1984; Linnhoff et al., 1994; Klemeš et al., 1997; Smith et al., 2000; Smith, 2005). A second edition of Linnhoff’s user’s guide was published by Kemp (2007). Applications of HI in the food industry were presented in Klemeš and Perry (2007a) and in Klemeš, Smith, and Kim (2008). Tan and Foo (2007) successfully applied the Pinch Analysis approach to carbon-constrained planning for the energy sector, and Foo, Tan, and Ng (2008) applied the cascade analysis technique to carbonfootprint-constrained energy planning. Another important part in process design and optimization is the synthesis phase of process flowsheets. From the earliest stages of PI there have been attempts to combine it with optimization (see, e.g., Giammatei, 1994). Such combining is usually performed after the targeting phase mentioned previously. Ideally, the structure of the entire process—and the configurations of the operating units within it—should be simultaneously designed and optimized, because the performance of each unit influences the others. The main source of complexity in this synthesis is the problem’s dual nature of being both continuous and discrete. There are several known methods for performing the task, including heuristic, evolutionary, and superstructure-based approaches. Two major classes of methods for process synthesis are heuristic and algorithmic (or Mathematical

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Chapter Two Programming) methods. Hybrid methods have also been proposed; these approaches incorporate heuristic rules as well as Mathematical Programming (MPR). Much as with any decision making, process synthesis (or design) is an activity for which no past experience can be ignored, especially when it comes to localized details of the design. The most popular approach is to create a superstructure for the network being designed and then choose the best possible solution network from the superstructure options.

2.4 Pinch Technology and Targeting Heat Recovery: The Thermodynamic Roots Furman and Sahinidis (2002) have compiled a comprehensive review of works tracing the development of the research on HENs in time. Their study shows that there was only mild interest in heat recovery and energy efficiency until the early 1970s, by which time just a few works in the field had appeared. But between the oil crises of 1973– 1974 and 1979 there were significant advances made in HI. Although capital cost remained important, the major focus was on saving energy and reducing related costs. It is exactly this focus that resulted in attention being paid to energy flows and to the energy quality represented by temperature. The result was the development of Pinch Technology, which is firmly based on the first and second laws of thermodynamics (Linnhoff and Flower, 1978). In this way HEN synthesis—one of the most important and common tasks of process design—has become the starting point for the PI revolution in industrial systems design. HENs in industry are used mainly to save on energy cost. For many years the HEN design methods relied mostly on heuristics, as necessitated by the large number of permutations in which the necessary heat exchangers could be arranged. Masso and Rudd (1969) is a pioneering work that defines the problem of HEN synthesis; the paper proposes an evolutionary synthesis procedure that is based on heuristics. An alternative HEN synthesis method is described in Zhelev et al. (1985), one that exploits synergies between heuristics and combinatorics. In this approach, several suboptimal networks are synthesized, and in most cases they are less integrated (consist of more than one subnetwork). A complete timeline and thorough bibliography of HEN design and optimization works is provided in Furman and Sahinidis (2002). The paper covers many more details, including the earliest known HEN-related scientific article: Ten Broeck (1944). The discovery of the Heat Recovery Pinch concept (Linnhoff and Flower, 1978) was a critical step in the development of HEN synthesis. The main idea behind the formulated HEN design procedure was to obtain—prior to the core design steps—guidelines

Process Integration and targets for HEN performance. This procedure is possible thanks to thermodynamics. The hot and cold streams for the process under consideration are combined to yield (1) a Hot Composite Curve representing, collectively, the process heat sources (the hot streams); and (2) a Cold Composite Curve representing the process heat sinks (the cold streams). For a specified minimum allowed temperature difference ΔTmin, the two curves are combined in one plot (see Figure 4.7), providing a clear thermodynamic view of the heat recovery problem. The overlap between the two Composite Curves represents the heat recovery target. The overlap projection on the heat exchange axis represents the maximum amount of process heat being internally recovered. The vertical projection of the overlap indicates the temperature range where the maximum heat recovery should take place. The targets for external (utility) heating and cooling are represented by the nonoverlapping segments of the Cold and Hot Composite Curves, respectively. The methodology is described in more detail in Chapter 4.

2.5 Supertargeting: Full-Fledged HEN Targeting After obtaining targets for utility demands of a HEN, the next logical step is to estimate targets for capital and total costs. Capital costs in HENs are determined by many factors, of which the most significant is the total heat transfer area and its distribution among the heat exchangers. Townsend and Linnhoff (1984) proposed a procedure for estimating HEN capital cost targets by using the Balanced Composite Curves, which are obtained by adding utilities to the Composite Curves obtained previously (see Figure 4.7). The HEN heat transfer area target is computed from the enthalpy intervals in the Balanced Composite Curves by using the heat transfer coefficients given in the HEN problem specification (assuming “vertical heat transfer” and “spaghetti-type topology”). Improvements to this procedure that have been proposed involve one or more of the following factors: 1. Obtaining more accurate surface area targets for HENs that exhibit nonuniform heat transfer coefficients (Colberg and Morari, 1990; Jegede and Polley, 1992; Zhu et al., 1995; Serna-González, Jiménez-Gutiérrez, and Ponce-Ortega, 2007). 2. Accounting for practical implementation factors, such as construction materials, pressure ratings, and different heat exchanger types (Hall, Ahmad, and Smith, 1990). 3. Accounting for additional constraints such as safety and prohibitive distance (Santos and Zemp, 2000).

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Chapter Two Cost estimation usually has a significant impact on a project’s predicted profitability. Taal and colleagues (2003) summarized the common methods used for cost estimation of heat exchange equipment and the sources of energy price projections. This paper showed the importance of choosing the right cost estimation method and a reliable source of energy price forecast when retrofit projects are evaluated for viability. Both retrofit and grassroots design projects require accurate cost estimates in the project’s early stages so that the correct choices are made. There are several methods available, most of which lead to FOB (Free On Board) cost estimates. As for operational costs, the range of possible future energy prices may prove crucial when the margins of a proposed design or retrofit project are analyzed. This is especially true for a large project that has a long payback period and consumes a lot of energy. Such projects are typical of plants in the chemical, petrochemical, refinery, and paper industries. Taal et al. (2003) include a brief review of oil and natural gas price projections reported by centers of excellence in the energy economics field. There are numerous forecasts, sometimes contradictory, but general trends can be observed. Some general insights in oil and gas price and production behavior are mentioned and refer to more detailed sources.

2.6 Modifying the Pinch Idea for HEN Retrofit Bochenek, Jezowski, and Jezowska (1998) compared the approaches of optimization versus simulation for retrofitting flexible HENs. This is an important work that should have generated additional research. Zhu, Zanfir, and Klemeš (2000) proposed a heat transfer enhancement methodology, for HEN retrofit design, from which HI could benefit substantially. This approach is worthy of wider implementation, especially in the context of retrofit studies. Heat Exchanger Network retrofit is a special case of optimization. In retrofit problems, one must accommodate an existing network with existing heat exchangers that are already paid for. This circumstance substantially alters the economics of the problem as compared with a new design. One example of this approach to retrofit was the paper of Tjoe and Linnhoff (1986), which suggested identifying heat exchangers with cross-Pinch heat transfer and, where appropriate, attempting to replace such heat exchangers with others that do not transfer heat across the Pinch, thereby reducing energy consumption. However, an ideal new design would not account for the existing HEN equipment and topological constraints. One method for overcoming these drawbacks is the Network Pinch (Asante, 1996; Asante and Zhu, 1997), which uses continuous nonlinear optimization to identify the bottlenecking heat exchangers within

Process Integration the existing network. The network bottleneck occurs at a heat exchanger, which constrains the load shifting to gain further improvement in heat recovery. At least one of the heat exchanger sides exhibits the minimum allowed temperature difference between the involved streams, and the corresponding point in the network’s temperature-load plot is referred to as the Network Pinch. To overcome this Network Pinch, the network structure must be modified. Possible modifications include the relocation of an existing heat exchanger, the addition of a new exchanger, or a change in the stream splitting arrangement. To identify the most promising modifications, the Network Pinch method uses MPR guided by thermodynamic insights. Nonlinear optimization is employed to evaluate the capital energy trade-offs and to produce a new optimal structure. This approach allows retrofit to be carried out one step at a time, leaving the designer in control to accept or reject suggested modifications at each step. There have been some successful practical applications of these targeting and retrofit methodologies. Pleşu, Klemeš, and Georgescu (1998) demonstrated the wide applicability of PI in the Romanian oil refining and petrochemical industry. In one of the first comprehensive retrofit case studies, Hassan, Klemeš, and Pleşu (1999) presented a PI analysis and retrofit suggestions for a fluid catalytic cracking (FCC) plant. Pinch Technology and its recent extensions offer an effective and practical method for designing the HEN for new and retrofit projects. Al-Riyami, Klemeš, and Perry (2001) demonstrated a HI retrofit analysis for the HEN of an FCC plant. Their study found significant room for improvement in the heat recovery process, and the new network was designed using the Network Pinch method.

2.7 Mass Exchange and Water Networks Water is widely used in the processing industries as an important raw material. It is also frequently used as a utility (e.g., steam or cooling water) and as a mass transfer agent (e.g., for washing or extraction). Large amounts of high-quality water are consumed in many industries that face strict requirements for product quality and the associated manufacturing safety issues. The processing industry is characterized by complex design and operation of storage and distribution systems for water management. Today’s industrial processes and systems that use water are subjected to increasingly stringent environmental regulations on the discharge of effluents. Increases in population and its quality of life have led to increased demand for freshwater. The rapid pace of these changes has made more urgent the need for improved water management. Adopting techniques to minimize both water consumption and wastewater

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Chapter Two discharge can considerably reduce demand for freshwater and also the amount of effluent generated by processing. For these reasons, the success of HI has inspired researchers to apply the Pinch and PI concepts to other areas—in particular, to mass exchange networks (El-Halwagi and Manousiouthakis, 1989). Wang and Smith (1994) developed a method for industrial water networks as a special case of mass exchange networks (see Figure 5.1). Their main objective was to minimize the consumption of freshwater and the disposal of wastewater simultaneously by maximizing the reuse of internal water, again exploiting the idea of recycling and reusing valuable streams and materials in order to save resources and reduce emissions. Wastewater can be further reduced by applying additional techniques for water regeneration that enable further reuse or recycling. For the case of a single contaminant, translating the method of Pinch Analysis to water minimization is straightforward: the water’s Composite Curve is used to construct a plot of contaminant concentration versus contaminant load. Extending the Water Pinch Analysis to multiple-contaminant problems is a complicated and difficult procedure. The principal issue concerns determining which contaminant to use on the Y axis when plotting the Composite Curves. Several approaches have been proposed. One option is to employ MPR, in which case Water Pinch serves as a preliminary visualization tool (Doyle and Smith, 1997). Foo, Manan, and Tan (2005) applied Water Pinch Analysis to synthesize optimal water recovery networks for batch processes. These authors introduced a numerical technique (time-dependent water cascade analysis) that has the advantage of clearly depicting the time-dependent nature of batch water networks. Majozi (2005) also employed mathematical modeling—the mixed integer nonlinear programming (MINLP) approach—to devise an effective technique for wastewater minimization in batch processes. Here, too, wastewater was minimized via application of reuse and recycle.

2.8

Benefits of Process Integration Heat recovery targeting for HEN synthesis problems is based on Composite Curves described in Section 2.4 (Linnhoff, Mason, and Wardle, 1979). The Composite Curves plot is a visual tool that summarizes the important energy-related properties of a process in a single view (see Figure 4.7). It was the resulting recognition of the thermodynamic relationships and limitations in the underlying heat recovery problem that led to development of the Pinch Design Method (Linnhoff and Hindmarsh, 1983), which is capable of producing maximally efficient heat recovery networks. As already discussed in this chapter, PI has been considerably expanded in scope since these initial applications. It is now also used for HEN

Process Integration retrofits, both water and combined water-and-energy minimization, as well as to minimize total site energy consumption—a process that includes Combined Heat and Power, locally integrated energy sectors, integration of renewables and waste-to-energy techniques, and combinatorial tools (P-graph and S-graph; see Chapter 7). In addition, recent applications have extended the PI approach to regional energy and emissions planning, financial planning, batch processes, and the targeting of other constrained resources, such as land, renewable energy, and emissions. In the wake of the initial breakthrough of Pinch Analysis for HEN synthesis, all these new PI applications follow the same simple logic: target setting should precede designing. In the most straightforward cases—such as HEN synthesis for Maximum Energy Recovery (MER) and water network synthesis for maximum water reuse—the targets can be interpreted as indicators of what a rigorous application could actually achieve. However, the applicability and benefits of PI are not limited to these straightforward cases. In fact, the target setting can be applied in various contexts and still yield enormous benefits in terms of reduced computational and project development time. Klemeš, Kimenov, and Nenov (1998) described several applications of Pinch Technology within the food industry, work that was further developed in Klemeš et al. (1999). This research showed that Pinch Technology can provide benefits far beyond oil refining and petrochemicals. The most important property of thermodynamically derived heat recovery targets is that they cannot be improved upon by any real system. Composite Curves play an important role in process design; for HEN synthesis algorithms, they provide strict MER targets. For process synthesis based on MPR, the Composite Curves establish relevant lower bounds on utility requirements and capital cost, thereby narrowing the search space for the following superstructure construction and optimization. The preceding observation highlights an important characteristic of process optimization problems, and specifically those that involve process synthesis and design. By strategically obtaining key data about the system, it is possible to evaluate processes based on limited information—before too much time (or other resources) are spent on the study. This approach follows the logic of oil drilling projects: potential sites are first evaluated in terms of key preliminary indicators, and further studies or drilling commence only if the preliminary evaluations indicate that the revenues could justify further investment. The logic of this approach was systematically formulated by Smith in his books on PI for process synthesis (Smith, 1995; Smith, 2005) and by Daichendt and Grossmann (1997), whose paper integrated hierarchical decomposition and MPR to solve process synthesis problems.

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Chapter Two

2.9 The Role of PI in Making Industry Sustainable Sustainability in the design and operation of industrial processes is becoming a key issue of process systems engineering. There are MPR tools for designing chemical processes that minimize costs (and thus maximize profits). These MPR formulations typically are highly complex; therefore, in practical applications, the original problem is usually decomposed into smaller problems that are solved sequentially. There are several definitions of sustainability. It can be defined as the capacity to sustain the viability of a given system. In this context, sustainable development implies that current actions should not harm future generations and that measurable indicators are needed to ensure compliance. For industrial processes, the relevant indicators are the rates of resource intake and effluent emissions. These factors are usually expressed in terms of “footprints” (De Benedetto and Klemeš, 2009)—for example, the carbon footprint (CFP) and/or water footprint (WFP) of a process. The sustainability of an industrial process depends on minimizing these footprints. For synthesis and design problems, the measured indicators should apply to the proposed system’s complete life cycle as part of a life-cycle assessment (LCA). In short, PI has a direct impact on improving the sustainability of a given industrial process. All PI techniques are geared toward reducing the intake of resources and minimizing the release of harmful effluents, goals that are directly related to the corresponding footprints. Hence, employing PI and approaching the targeted values will help minimize those footprints. Footprint considerations, however, are only part of an industry’s ultimate indicator—that is, its economic performance. This metric takes the form of either cost or profit, depending on the selected system boundaries. Thus, no matter how environmentally attractive a given project may be, it will probably not be implemented unless doing so is economically feasible. There are several ways to merge the objectives of sustainability and profitability. The two most popular are (1) expressing footprints in strictly economic terms and then folding them into the cost or profit objective function; and (2) employing multiobjective optimization, whereby footprint and economic indicators are evaluated in parallel as objectives to be achieved.

2.10

Examples of Applied Process Integration In this section, four examples illustrate the potential of PI to reduce not only resource demand but also operational and capital costs. The problem areas vary widely, yet in each case the application of the PI techniques yields significant benefits. Only the main problem points and outcomes are described here; see Chapter 11 for more details.

Process Integration

Petrochemicals: Fluid Catalytic Cracking Process The FCC unit is a major process element in oil refineries, and improvements in yield and efficiency have been attempted over the years in response to various external drivers. Retrofitting the HEN associated with an FCC usually leads to improved energy recovery and thus to reduced energy use and/or increased throughput. In this example, the HEN of the FCC process includes a main column and a gas concentration section (Al Riyami, Klemeš, and Perry, 2001). The particular FCC plant considered had 23 hot streams and 11 cold streams, and the associated cost and economic data required for the analysis were specified by the refinery owners. The task was to analyze the existing process and then propose a HEN retrofit plan for improving energy recovery. Incremental area efficiency was used for the targeting stage of the retrofit design, which was carried out using the Network Pinch method (Asante and Zhu, 1997) consisting of a diagnosis stage and an optimization stage. In the retrofit, four heat exchangers were added and one existing exchanger was removed. The resultant design produced energy savings of 8.955 MW or 74 percent. This translated into a 27 percent decrease in the plant’s utility bill for an annual savings of $2,388,600. The modified HEN required an investment of $3,758,420, so the payback period was less than 19 months.

Energy Integration of a Hospital Complex Herrera, Islas, and Arriola (2003) studied a hospital complex that included an institute, a general hospital, a regional laundry center, a sports center, and some other public buildings. The diesel fuel used to generate the steam required for the complex amounted to 75 percent of its total energy consumption and 68 percent of its total energy cost ($396,131 in 1999). The Pinch Analysis that was performed estimated the minimum need for external heating at 388.64 kW. Because the actual heating used was consuming 625.28 kW, there existed a potential energy savings of 38 percent.

Sunflower Oil Production As reported by Klemeš, Kimenov, and Nenov (1998), an oil production process operated with a minimal temperature difference of 65°C at the Process Pinch has been analyzed. The external heating required by the system was provided by two types of hot utilities, and the required external cooling was provided by two cold utilities. The study resulted in increasing heat recovery and reducing the minimum temperature difference to 8–14°C. This reduced the hot and cold utility requirements and eliminated the need for water steam and cooling water, which considerably simplified the overall design.

A Whisky Distillery In a study by Smith and Linnhoff (1988), the authors found that steam was being used below the Process Pinch; this resulted in unnecessarily

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Chapter Two high utility usage by the distillery. The steam in question resulted from the use of a heat pump, and so the steam below the Process Pinch was eliminated by reducing the heat pump’s size. Although this approach required that the steam now be used for process heating above the Process Pinch, overall energy costs were still reduced owing to the reduced compressor duty.

2.11

Summary This chapter offered an introduction to and an overview of the field of PI, its HI roots, the expansion of its application areas, and the evolution of process optimization methods toward combining PI techniques and insights with the tools of MPR. The chapter discussed the philosophy of PI as well as its contribution to sustainable development and the economic efficiency of projects. There is a wealth of useful information on these topics, and a number of excellent sources of further information are described in Chapters 13 and 14.

CHAPTER

3

Process Optimization

T

his chapter deals with process optimization: its definition, goals, and application areas within sustainable industrial process design and integration. The aim is to provide information on how to formulate sustainability tasks as optimization problems and on what tools to employ for solving them. The chapter begins with a brief description of the general framework for model building and optimization; this is followed by basics of optimization problems and their classes as well as descriptions of the most common algorithms for solving optimization problems. Finally, the chapter discusses how to build models efficiently, how to handle complexity, and how to ensure model adequacy and sufficient precision. The details of computational implementations of optimization solvers and other software tools are given in Chapter 9.

3.1

Introduction Building and operating industrial processes entail costs and environmental impacts. Emissions and effluents include: gaseous waste streams, which may harbor CO2, SOx and NOx; wastewater and various aqueous streams; and flue gases. When attempting to improve the environmental and economic performance of process systems, it is important to keep in mind that the processing paths, which connect the various system inputs and outputs, usually interact with each other. Therefore, minimizing resource demands and environmental impacts is greatly facilitated by properly modeling the process systems and then deciding which designs and operating policies to pursue—in what priority and to what extent. Maintaining a balance between model accuracy and simplicity is necessary in order to derive meaningful results with minimal computational expense. A system model can be created for different purposes. A lumped steady-state model (i.e., one that neglects variations in time and space) will contain only algebraic equations. To simplify the problem, steady-state models assume that the operating units are “black boxes” or “gray boxes” (a black box is a model that represents an empirical process in terms of its input, output, and transfer parameters but does not describe any internal physics; a gray

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Chapter Three box is a model that incorporates a physical representation, although some of the physics is approximated—see, e.g., Hangos and Cameron, 2001). This approach is appropriate for optimizing complex systems. If time variability has to be accounted for then steady-state modeling can be applied to a set of operating periods, each of which is characterized by its own fixed parameters.

3.2 Model Building and Optimization: General Framework and Workflow A good process model should contain a thorough conceptual description of the involved phenomena, unit operations, actions, events, and so forth. Usually this description involves text, flowsheets, and structural diagrams. Additionally, IT-domain diagrams—for example, UML diagrams—can be used (“UML” is a specification of the Object Management Group; UML, 2010). The UML diagrams include class, object, package, use case, sequence, collaboration, statechart, component, and deployment diagrams. A good process model should also contain a sufficiently precise mathematical description. The mathematical relationships are used to reflect not only physical laws but also technological constraints and company rules. Mathematical models include algebraic equations of some form (i.e., equalities or inequalities) and may be supplemented with dynamic modeling, which uses differential equations to capture variations in time, as well as states and actions to express operational procedures and other dynamic relationships of algorithmic nature. Structural information is also an essential feature of process network models. When translated to Mathematical Programming (MPR) models, such information is expressed by integer (mostly binary) variables. An efficient alternative to representing superstructures with binary variables is the P-graph and its related framework (Friedler et al., 1992b), discussed in Chapter 7. An efficient computational implementation of the mathematical description may take the form of a stand-alone compiled application (e.g., PNS Editor, 2010) or may be modeled within a popular environment for process and mathematical calculations. Examples include MATLAB (MathWorks, 2009), Scilab (2009), simulation and optimization tools tailored for the process industry (AspenTech, 2009c), Modelica (2009a; OpenModelica, 2010), Honeywell UniSim (Honeywell, 2010), and the open-source DWSIM (2010). All model components have to be well synchronized to provide appropriate user interfaces and sufficient visual aids to help understand the process and the optimization results. Models often include only the computational implementation with some mathematical descriptions, but a much better practice is to start with the concepts before deriving the mathematical relationships

Process Optimization and then finally implementing the model computationally. In the course of formulating the mathematical and implementation components, it may be necessary to make some corrections to the conceptual and/or mathematical components.

3.3 Optimization: Definition and Mathematical Formulation 3.3.1 What Is Optimization? Optimization can be applied to different tasks: new system design, the synthesis of a new processing network, and the retrofit design and operational improvements in heat exchanger, reactor, and separation networks. Optimization is employed to find the best available option. An objective function consists of a performance criterion to be maximized or minimized. The system properties that determine this function are of two types: 1. Parameters—a set of characteristics that do not vary with respect to the choice to be made 2. Variables—a set of characteristics that are allowed to vary Some of the variables are specified by the decision maker or are manipulated by the optimization tools; these are referred to as specifications or decision variables. The remaining variables are termed dependent variables, and their values are determined by the specifications and the system’s internal relationships. The objective function can be formulated in terms of a single variable or a combination of dependent and decision variables. The value of the objective function can be changed by manipulating the decision variables.

3.3.2 Mathematical Formulation of Optimization Problems Optimization tasks in industry include increasing heat recovery, maximizing the efficiency of site utility systems, minimizing water use and wastewater discharge, and other tasks. The formulations that are used to solve such optimization problems are known as mixed integer nonlinear programs (MINLPs). However, they are frequently linearized to yield the more tractable mixed integer linear programs (MILPs), and some can be further simplified and solved via linear programming (LPR). In general, optimization problems can be formulated as summarized in Table 3.1. The continuous and discrete domains, together with the constraints, define the feasible region for the optimization. This region contains the set of options from which to choose. The value of the function F depends on the values of the decision variables.

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Chapter Three Minimize (or maximize) F(x, y) where

x ∈ Rn (continuous variables) y ∈ Z n (integer variables)

subject to h(x, y) = 0 g(x, y) ≤ 0 TABLE 3.1

Objective function, performance criterion Continuous domain Discrete domain Equality constraints Inequality constraints

Generic Optimization Problem

Continuous variables are used to model properties (e.g., flow rates and chemical concentrations) that vary gradually within the feasible region. Integer variables are used to model the status (ON versus OFF) of operating devices as well as the selection/exclusion of options for operating units in synthesis problems. Using only the problem formulations, it is possible to generate many combinatorially infeasible sets of the integer variable values, which are later analyzed by the optimization solver. Especially for larger problems, it’s a good idea to eliminate these infeasible combinations from the search space or to build into the optimization solver a mechanism for avoiding them (Friedler et al., 1996). The type of the objective function F dictates which extremum— the minimum or the maximum—to seek. Common performance criteria are to minimize the process cost or to maximize the profit. Because some process subsystems (e.g., water networks) do not usually generate useful product streams, no revenue is directly realized and so minimizing the total annualized cost is used instead as an objective function. For complete production systems and supply chains the objective is usually to maximize the profit. Thus, additional variables (reflecting sales and customer behavior) and their relationships may be added to the formulation. Equality constraints stem not only from material and energy balances but also from constitutive relations that normalize the stream compositions to unity. The balances include those for total flow rates, balances of the chemical components, and energy balances of heat exchangers, boilers, and turbines. Inequality constraints stem from limitations on concentrations, flow rates, temperatures, pressures, throughput, and so forth. One example of a constitutive relation is calculation of the fluid heat capacity flow rate from its mass flow rate and specific heat capacity.

3.4 Main Classes of Optimization Problems This section discusses methods that can be applied to detect optimality and solve optimization tasks. Choosing a particular

Process Optimization method should be based on a clear understanding, and toward this end it is useful to bear in mind three aspects of optimization problems: 1. An optimization problem is convex if it minimizes (or maximizes) a convex objective function and if all the constraints are convex (Williams, 1999). 2. An optimization problem is linear if its objective function and all the constraints are linear; note that all linear optimization problems are also convex (Williams, 1999). 3. A variable that can assume only integer (whole number) values is an integer variable; integer variables that are constrained only to values of 0 or 1 are binary variables. Optimization problems are classified in terms of the following specific features: • Objective type: Minimization or maximization problems. • Presence of constraints: Unconstrained versus constrained. Most practical tasks involve the formulation of constrained optimization problems. • Problem convexity: Convex versus nonconvex. • Linear and nonlinear problems: This aspect depends on the nature of the objective function and/or the constraints. Most process optimization problems are bilinear (i.e., containing products of two optimization variables), for example, they feature componentwise mass balances involving products of mass flow rates and concentration and enthalpy balances involving products of mass flow rates and enthalpies. • Absence of integer variables: In such cases the entire problem is continuous and so linear programming (LPR) or nonlinear programming (NLP) models are employed. • Presence of integer variables: In such cases the problem is referred to as “integer.” Integer problems are further subdivided into pure integer programming (IP) models, which involve only integer variables; mixed integer linear programming (MILP) models, which involve linear relationships with both integer and continuous variables; and mixed integer nonlinear programming (MINLP) models, which involve nonlinear relationships with both integer and continuous variables. Further details on these classifications and their properties can be found in Floudas (1995) and Williams (1999). The most important

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Chapter Three factors are linearity and the existence of integer variables. There are two main reasons for the significance of these factors: 1. Continuous problems are solved by using simpler methods that incorporate gradient or other search mechanisms. The presence of integer variables introduces combinatorial complexity caused by the need to build search trees that branch through the integer variables. 2. Nonlinearity introduces a different type of complexity. Whereas linear problems (LPR and MILP) have been shown to be convex (Floudas, 1995; Williams, 1999), the convexity of nonlinear problems (NLP and MINLP) must be evaluated on a case-by-case basis. Such problems are generally assumed to be nonconvex until proven otherwise.

3.5 Conditions for Optimality One of the most popular methods for handling optimization formulations is the use of MPR solvers. They usually take standardized input in the form of matrices of variables, parameters, and equations, after which they explore the search space, using local search and gradients, to reach an optimal solution.

3.5.1 Conditions for Local Optimality When employing local search (e.g., gradient-based) algorithms, the desired extremum (minimum or maximum) needs to be located and proven. The optimality condition usually employed by solver algorithms is based on the mathematical definition of an extremum. For finding a minimum, the definition requires the existence of a point in the search space such that any small deviation from that point, in any direction within the search space, will result in an increase of the objective function value or in keeping it the same:







F x * , y * d F  x , y ,   x , y  vicinity of x * , y *



(3.1)

Further details are given in specialized textbooks on optimization (see, e.g., Edgar and Himmelblau, 1988; Floudas, 1995; Luenberger and Ye, 2008). Rigorous definitions can also be found by searching the Web for “KKT optimality conditions” (aka Karush–Kuhn–Tucker conditions, an extension of the method of Lagrange multipliers).

3.5.2 Conditions for Global Optimality Additional conditions are applied to attain global optimality when using local search algorithms, which in this case require the problem

Process Optimization to be convex. For linear problems (e.g., MILP), the locally optimal solution is guaranteed to be global—in other words, the best possible. Another advantage of the linear model is that linear solvers, unlike with nonlinear ones, do not require initialization with a feasible solution. Nonlinear problems are much more difficult to solve, and attaining feasibility of the solutions is a significant issue. Any result obtained guarantees global optimality only if the optimization problem is shown to be convex (Williams, 1999).

3.6 Deterministic Algorithms for Solving Continuous Linear Optimization Problems The best-known algorithm for LPR problems is the simplex algorithm (Dantzig, 1951; Dantzig, Orden, and Wolfe, 1954). It solves LPR maximization problems by constructing a feasible solution at a vertex of the search polyhedron and then walking along the edges of the polyhedron to other vertices with successively higher objective function values. Although this algorithm is efficient in general, in some cases it may require exponential time to find the optimum. Khachiyan (1979) proposed a method that, in the worst case, finds a solution in polynomial time for the worst case. Today, the LPR problems are usually solved using one of two methods: 1. Revisions of the simplex algorithm: This algorithm has been developed almost continuously over the years since its initial formulation, starting with the revised Simplex Method of Dantzig and Orchard-Hays (1953). A thorough consideration of the simplex algorithm and its computational techniques is given in Maros (2003b). Modern LPR solvers use algorithms that flexibly solve both continuous and integer linear problems. 2. Interior point methods: In contrast to the simplex algorithm, which finds the optimal solution by traversing points on the boundary of the feasible region, interior point methods move through the interior of the feasible region. One such method (see Mehrotra, 1992) is used by MATLAB.

3.7 Deterministic Algorithms for Solving Continuous Nonlinear Optimization Problems Nonlinear programming is used to solve continuous nonlinear problems. A common feature of all deterministic search methods is that, starting from a current solution point, they perform an iterative search for a better feasible solution within the vicinity of the current

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Chapter Three one, repeating this action until no further solution improvement is possible. This strategy means that the methods find only local optima, so there is no guarantee of global optimality. Although modern optimization software packages are capable of solving constrained problems, they are mostly based on the search techniques developed for unconstrained optimization.

3.7.1 Search Algorithms for Nonlinear Unconstrained Problems Many methods have been developed for performing local search for the minimum of an objective function (Luenberger and Ye, 2008). Deterministic search algorithms mainly assume that the objective function is minimized and use the concept of descent: a series of iterations are performed that aim reducing the objective function value at each iteration. A thorough review of the deterministic search algorithms for optimization and their performance, as applied to chemical process models has been provided elsewhere, for example, Klemeš and Vašek (1973). Such methods include pattern search, the Rosenbrock method, and conjugate gradients. All descent-based algorithms rely on a common general strategy. First, an initial solution point is chosen. Then, a rule-based direction of movement and a step size are determined and executed. At the new point, a new pair of direction and step size are determined, and the process is repeated until the desired convergence is achieved. The main difference between the various search algorithms is in the rule applied for determining the iteration steps. When the search domain is a given line, the process of determining the function minimum is known as a line search. Higher-dimensional problems are solved by executing a sequence of successive line searches. The two simplest line search algorithms are the Fibonacci method (e.g., Avriel and Wilde, 1966) and the golden section method (e.g., Kiefer, 1953). Both algorithms search over a fixed interval and assume that the function is unimodal within it. The golden section algorithm has a linear convergence rate of dk+1/dk = 0.618. Another line search algorithm is the Newton method, which is based on the additional assumption of function smoothness; this technique achieves even faster convergence than the golden section one. There are also other line search algorithms that are grouped together as curve-fitting methods. Another important search algorithm—one that is applicable to multidimensional function domains—is the method of steepest descent or gradient method. Its update rule derives the new step based on the gradient information in the current point, identifying the direction of the fastest decrease of the objective function. This is one of the oldest and best-known function minimization methods. Hence it is often used as a benchmark against which the performance

Process Optimization of other methods is measured. See Luenberger and Ye (2008) for additional information.

3.7.2 Algorithms for Solving Constrained Nonlinear Problems Many algorithms for constrained problems proceed in two main steps: (1) The constrained problems are transformed into equivalent unconstrained ones, and then (2) the modified problems are subjected to unconstrained search algorithms. Groups of such algorithms include primal methods, penalty and barrier methods, and primaldual methods. The primal algorithms search for the optimal solution directly through the feasible region. For a problem with n variables and m equality constraints, primal methods work within the (n − m)dimensional feasible space. Each point in the process is feasible, and the value of the objective function constantly decreases. Thus, a feasible solution is guaranteed even if the search is interrupted before it finishes. Most primal methods do not rely on special problem structure (such as convexity), so they are applicable to general NLP problems. The weaknesses of primal algorithms are their requirement that an initial feasible solution be found or specified and their slowness (or even failure) to converge in the case of nonlinear constraints. Penalty and barrier methods utilize unconstrained approximations of the constrained optimization problem. Penalty methods add a penalty term to the objective function, which results in a high cost if constraints are violated. Barrier methods instead add a term that favors points interior to the feasible region over those near the boundary. There are two major issues with applying these methods. First, it is important to ensure the accuracy with which the unconstrained NLP problem being solved approximates the true, constrained one. Second, it is possible that the penalty or barrier term may dominate the objective function, skewing the problem to such a degree that the feasible solutions found are not actually optimal.

3.8 Deterministic Methods for Solving Discrete Problems All integer programming problems (pure IP, MILP, and MINLP) possess combinatorial features. The first solution methods used cutting planes (i.e., added constraints to force integrality), and various algorithms have been devised on this basis. The effective approach has been to divide the problem into a number of smaller problems, a method known as branch and bound. This is a strategy of problem decomposition: it aims to partition the feasible region into more manageable subdivisions and then, if required, into further subdivided partitions. The method was proposed by Land and Doig (1960) for solving LPR problems and has since evolved to a point where it can

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Chapter Three be used to solve IP and MIP problems. The original large MIP problem is divided into a number of subproblems, called nodes, which form an enumeration tree. The algorithm starts from a main node and progresses toward the so-called leaves, adding nodes to the current solution or discarding them as necessary. In this process, an important role is played by the bounding function, which (in the case of objective minimization) provides a lower bound on the remaining part of the problem under the current branch. Thus, if the lower bound on the current subproblem node is higher than the current best solution, then the algorithm can safely discard (prune) the node and all its subnodes. More information on IP solving algorithms can be found in Nemhauser and Wolsey (1999).

3.9 Stochastic Search Methods for Solving Optimization Problems An alternative to deterministic algorithms are those that employ stochastic sampling of the search space and hill climbing: pushing the algorithm to lower objective function values (assuming minimization) by allowing temporary increases in the objective function value. The main advantage of stochastic search methods is that their search is not confined in the neighborhood of a given current solution, which means there is a higher probability of finding the global optimum. Such techniques have proven to be successful in applications—for example, process design and synthesis studies—where the computational requirement for single samplings is modest and the time frame for producing a solution is more relaxed. Their major limitation is that many iterations are required in order to assure some degree of optimality. This is because the algorithms blindly evaluate even infeasible combinations of variable values, especially for the simulated annealing variants. Simulated annealing (SA) is the most prominent stochastic search method (Kirkpatrick, Gelatt, and Vecchi, 1983). An interesting application is the GAPinch toolbox for MATLAB (Prakotpol and Srinophakun, 2004), which implements a genetic algorithm (GA) search to solve MINLP network synthesis problems involving water reuse. Another promising development is the use of the GA framework to optimize schedules and supply chains (Shopova and Vaklieva-Bancheva, 2006). Ant colony optimization (Zecchin et al., 2006) and Tabu search (Cunha and Ribeiro, 2004) have been applied to process design and operation. Other examples of stochastic search methods include the following: 1. McKay, Willis, and Barton (1997) used genetic programming (GP) to identify steady-state models of integrated chemical processes.

Process Optimization 2. Manolas et al. (1997) applied GA techniques to the optimal operation of industrial utility systems. 3. Castell et al. (1998) described a novel GA application to optimize process layout. 4. Genetic algorithms have been proposed for the synthesis of Heat Exchanger Networks (HENs) and other processing systems (Ravagnani et al., 2005; Xiangkun et al., 2007; Fieg, Xing, and Jeżowski, 2009); the paper by Xiangkun and colleagues presents a hybrid GA-SA method. 5. Ahmad et al., (2008) proposed that SA be used for synthesizing Heat Exchanger Networks. This approach employs a completely evolutionary strategy, starting from a trivial network topology that connects all hot streams to coolers and all cold streams to heaters.

3.10

Creating Models The procedure for building a process model is illustrated in Figure 3.1. The modeling begins with accumulating sufficient information about the process—in order to develop an understanding of the elements and the relationships between them—and proceeds to formulating a mathematical description of the process that is implemented on a computational platform. A distinctive characteristic of the procedure is its iterative nature. The mathematical modeling

BEGIN YES Conceptual modeling

YES

Mathematical modeling

Need corrections?

NO Computational implementation NO END

FIGURE 3.1

Model creation procedure.

Need corrections?

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Chapter Three often leads to changes in the conceptual model; the result is an iterative feedback loop, as shown in the figure. A similar correction loop is also present at the output of the implementation block. The discussion that follows addresses only those activities in Figure 3.1 that involve conceptual and mathematical modeling.

3.10.1

Conceptual Modeling

Conceptual modeling involves collecting and organizing essential information about the phenomena in the process under consideration. This step is often referred to as data extraction (Williams, 1999). The process operating units are described along with the relevant features of their behavior. The important constraints for the units’ capacities and other limitations are identified and added to the description, as is topological information about the process network. The main purpose of this description is to serve as an interface between the process operators and the modelers. Therefore, it is important that the description be concise enough that modelers can efficiently grasp the workings of the complete system. That being said, the description must contain sufficient detail to complete the study.

Extracting Data About the Operating Units When a production process is modeled for the purpose of Process Integration, the data extraction involves four main steps: 1. Description of the process operating units and their interconnections; creation of a flowsheet that reflects this description. 2. Identification of the heating and cooling needs of the process through use of the flowsheet and related data about the operating units. 3. Definition of the Heat Integration process streams: identifying for each stream the values for its heat load, as well as the supply and target temperatures. Some process streams may need to be segmented. This is done if the specific heat capacity of a given process stream varies significantly within the interval between its supply and its target temperature. 4. Analysis of the collected data. If the goal is to minimize water use and wastewater discharge, then the various water-using operations are analyzed and their relevant properties are recorded in some standard form. The most popular way to express the water requirements (Wang and Smith, 1994; Kuo and Smith, 1997) of an operation is in terms of the limitations on (1) inlet and outlet concentrations of different contaminants and (2) flow rates of the water to be consumed. This topic is discussed in more detail in Chapter 12.

Process Optimization

Network and Topology Data Identification Obtaining network-related information is needed to account for constraints that are related to the system topology and to the limits imposed by operating units on the suitability of various process streams to serve as inputs or outputs. In water networks, such considerations include the acceptability (or unacceptability) of using the water output from some operations as inputs for other operations. For instance, the final washing of sugar crystals in sugar production would require pure water, and for this the outputs from other waterusing operations would be unacceptable. On the otherhand, used water from blanching might be perfectly acceptable for the initial washing or rinsing of fruits. This type of information is used to formulate additional constraints on the compatibility of different process streams. When supplied to automated process optimization algorithms, these constraints serve to eliminate a number of infeasible combinations of process units. When building pure MPR models (Williams, 1999), network-related information is transformed into explicit mathematical constraints involving expressions with binary selection variables. When using the graph-theoretic approach and/or the P-graph framework (Friedler et al., 1993) to construct a process model, such information is explicitly encoded in the P-graph building blocks (materials and operations) and is then used by algorithms that generate only those topologies that are combinatorially feasible.

3.10.2

Mathematical Modeling of Processes: Constructing the Equations

After the conceptual basis has been established, it is time to begin constructing the explicit mathematical formulations of the problem. The standard procedure in this regard is first to build a superstructure—one that incorporates all possible options and combinations of operating units—and then to reduce the superstructure via optimization techniques. In this context, a superstructure is the union of several feasible flowsheets (see Figure 6.2 for an example of a water reuse network superstructure). When this union includes all possible flowsheets, the superstructure is called the maximal structure (Friedler et al., 1993) or the hyperstructure (Papalexandri and Pistikopoulos, 1996). There are two basic approaches to formulating the superstructure and subjecting it to reduction optimization. 1. Explicit formulation of a superstructure by the design engineer, followed by translation of that structure into an integer programming model: The generated problem is then solved by the corresponding MPR algorithm. Popular codes for solving MILP problems are OSL (GAMS, 2009) and CPLEX (ILOG, 2009); both are included in such commercial optimization software packages as GAMS (2009). If the model does not

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Chapter Three involve choices between structural options and involves decisions on flow rates and capacities only, then continuous optimizers (LPR or NLP) can be used. 2. Automated generation of the maximal superstructure, followed by enumeration of all feasible network topologies using the P-graph framework. The unit operations can be described in terms of (a) the input to the automated procedure, (b) the compatible connections between them, and (c) the corresponding process and cost information. More details are provided in Chapter 7. The construction of a process network model begins with formulation of the mass balances. The following key points should be kept in mind: • Mass balances can be of two types: overall and componentwise. Overall balances are performed over the total contents of the input and output streams of a process unit. For steadystate models of continuous processes, this content is usually expressed as a mass-based flow rate (e.g., in units of kg/s, kg/h, or t/h). Componentwise mass balances reflect the mass conservation principle between the inlet and outlet streams for individual chemical components (or pseudocomponents). • For a given operating unit, the set of all componentwise mass balances is exactly sufficient for completely characterizing the material flows into and out of the unit (adding the overall balance could lead to an “overspecified” system of equations). However, if using the overall material balance is critical to the system model, then the overall balance can be used in place of one of the componentwise balances. • In some cases, tracking all chemical species in various process streams is not necessary. This is true for water networks in which mass balances are written for the water flow rates and for the analyzed contaminants. However, an incomplete list of the material species contained in the water streams will naturally result in incomplete mass balances (Smith, 2005). When complete results are necessary, rigorous simulations of the optimized system must be performed. • The componentwise mass balances of stream mixers and the more complex operating units involve bilinear terms that reflect products of the stream flow rates and the component concentrations. In this case, the result is an NLP or MINLP problem. If either the concentrations or the flow rates are fixed then the model could be linear (an LPR or MILP problem), which would make for an easier computation that might guarantee global optimality. Although such an approach is

Process Optimization often viable, additional analyses are required to ensure that the linearization does not result in an inadequate (inaccurate) model. Similar problems also exist for Heat Exchanger Networks, where nonisothermal mixing leads to equations containing bilinear terms: products of mass flow rates and enthalpies. Process-specific constraints are also included in the optimization problem. The mass balances are supplemented in the model by lower and upper bounds on the stream flow rates and component concentrations. Another source of constraints is the temperature feasibility of interequipment connections. For example, water coming from a blanching operation may be too hot to be used for washing fresh fruits and so may require cooling (perhaps by mixing with a colder stream) before this use; alternatively, this may be rejected as an unacceptable connection, leading to a forbidden match. In MPR, such constraints usually contain integer variables. A frequent problem when synthesizing process networks is obtaining extremely low flow rates for some interconnections. When the model to optimize accounts for the complete capital costs, this problem is less likely to appear. However, if capital costs are underestimated (or disregarded) for some reason, then operating costs may dominate, resulting in “degenerate” solutions with impractically small flow rates. Practical solutions require reasonably accurate estimates of the capital cost, especially if there are fixed costs. A more straightforward option is to stipulate a lower bound on all network flow rates. Another important part of creating a process model is identifying the energy needs of various operating units. It is crucial to account for the heating and cooling needs of the process operations, and these are established by formulating enthalpy balances (Linnhoff et al., 1982). Most process streams need to be transported between the operating units and also moved through them, and such transport involves overcoming certain pressure drops (for fluids) and performing mechanical work (for solids). These operations require mechanical shaft power, which can be supplied by direct-drive machines or electrical motors—elements that define the power requirements of a process. In many cases, additional equations are needed (e.g., constitutive relations as well as calculations of reaction rates and equilibriums).

3.10.3

Choosing an Objective Function

The objective function to choose depends on the goal of the optimization. It is possible to choose from a number of criteria, including (1) maximizing profit; (2) minimizing operating cost; (3) minimizing total annualized cost (TAC); (4) minimizing consumption of certain resources or consumption per unit of product;

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Chapter Three and (5) minimizing the system’s total environmental footprint or the footprint per unit of product. It is frequently necessary to optimize more than one criteria. There are three main approaches to this task (Ehrgott, 2005): 1. Choose one criterion for formulating the objective function; then add the other criteria as constraints to the problem. 2. Combine all the criteria into one objective function by summing them up, where each criterion is weighted with a given coefficient. 3. Perform a multicriteria optimization, accounting explicitly for the conflicts between the chosen objectives (criteria).

3.10.4 Handling Process Complexity Process synthesis and process design tasks—when performed on real-life, industrial-scale problems—tend to involve substantial number of operating units. Examples can be found in many areas: • Synthesizing Heat Exchanger Networks involves a large number of possible combinations of potential heat exchangers. Thermodynamic and process-related constraints usually reduce this number, but even then the complexity remains significant. • Water subsystem design is no exception, and problems with 20 or more water-using operations are common (Bagajewicz, 2000; Thevendiraraj et al., 2003). This number leads to high levels of combinatorial complexity. In a superstructure, each water-using operation (and each intermediate water main) defines at least one mixer. If the number of water-using operations is denoted by Nop, then there can be no fewer than Nop corresponding binary variables in the network superstructure, and the number of combinations of binary variable values to be examined by the corresponding MIP solver would equal 2Nop. Thus, for 20 operations there would be more than a million (106 = 1,000,000) possible combinations. When using MPR superstructure models directly, the number of binary variables is dictated by the number of the candidate operating units. In the worst case, the solution algorithm will have to examine the entire search space, which depends exponentially on the number of the binary variables. One modeling strategy that reduces the search space by several orders of magnitude is to use the Maximal Structure Generation (MSG) and Solution Structures Generation (SSG) algorithms of the P-graph framework (Friedler et al., 1993). These algorithms effectively discard all infeasible combinations of the binary selection variables and retain only the feasible ones.

Process Optimization Another popular technique in process design and software development is modularization or encapsulation. The complexity management efforts in information technology and process modeling led to development of the concepts of object-oriented modeling (see, e.g., Modelica, 2009a; UML, 2010) and object-oriented programming (e.g., C++, C#, Java, Delphi). With these modeling concepts, a number of related objects or operations can be grouped together and represented as a single object or operation. Similarly, flowsheeting and simulation software may offer the option of representing a distillation column as a single operating unit at the level of the entire flowsheet while still allowing simulation of the column at the local level; such a facility is available, for example, in gPROMS (PSE, 2009) and HYSYS (HYSYS, 2010). The key to object-oriented thinking is the principle of information hiding, according to which every object should conceal as many details as possible about its own functionality and provide to other objects only the information relevant to interactions with them. Hence, the interface describes the bundle of information items that are defined as being available to an external object. An example of applying information hiding in water network design is the abstraction of the detailed information about water-using operations into only three relevant pieces of information for each operation and contaminant: the limiting inlet and outlet concentrations and the limiting flow rate (or contaminant load). This bundle of information thus constitutes the operation’s interface to the water minimization problem. Efficiently managing the model and problem complexity is greatly facilitated by the practice of documenting the complete modeling process and optimization results, including their interpretation. It is best to document all stages, starting from the conceptual modeling and ending with the computational implementation and obtained results. All this documentation should be systematic so that the reasoning and results can be clearly understood and traced back to their roots. This style of documentation is extremely useful and makes the work of teams and individual engineers smoother and more efficient in the long run. Another important tool for managing complexity is targeting, which reveals limitations in the underlying design or operation task to which the optimization is being applied. With proper targeting it is possible to obtain an upper bound on system performance and/or a lower bound on system cost. In fact, it is also possible to calculate practically achievable targets: • For water systems, current targeting practices mainly yield the first type of estimate: the maximum possible amount of water reduction. • For HEN synthesis, the Maximum Energy Recovery (MER) targets can be established, and HENs achieving them also

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Chapter Three feature reasonable costs. However, this is seldom the global minimum for the total annualized cost (i.e., the sum of annual operating costs and annualized investment costs). The logic behind evaluating a system in terms of the upper bound on its performance is this: if the best possible system performance is still insufficient to satisfy the specified requirements, then no further time and effort should be spent on designing that system. The next section gives more details on the use of targeting to managing design problem complexity.

3.10.5 Applying Process Insight Mathematical tools are absolutely necessary for optimizing the design and operation of industrial processes. However, meaningful and applicable results are obtained only when process insight is used to guide the model building, the optimizing, and the interpretation of results. Each optimization problem has its own particular features. For example: • The processing of fruits for canning imposes different water requirements and practices from those for the processing of poultry. • When designing HENs, the various underlying process operations that need cooling or heating should be properly examined for data extraction. In some cases, process knowledge may aid in the lumping of different heating/cooling needs, thereby simplifying the flowsheet. Process knowledge is also employed when partitioning properly into segments a process stream whose heat capacity flow rate varies widely. Every specific requirement discovered in the iterative process of model improvement should be thoroughly documented and implemented in the model—for instance, in the form of constraints or simplifying assumptions. A good practice is to perform targeting for the desired application: a heat recovery problem, water management, a separator network, or reactor network design. Targeting provides information on potential performance. Targeting procedures have been developed and well tested for a number of applications and domains (see Chapter 2 for a review). The benefits of using variants of Pinch Analysis or other targeting are twofold. First, the designer can estimate the best possible performance of the system by using simple models and calculations, even before using rigorous design procedures, saving valuable time. The obtained targets can be used in preliminary sensitivity studies to determine which operations and units should be included in the design and which should be left out. This approach can greatly

Process Optimization simplify network design if the number of candidate operations is large and the targets can be used as guides in the network synthesis. Usually the engineer aims either to achieve the targets exactly or to approach them closely with the final design. If the targeting model is too idealized, then the estimates produced will serve as loose performance or cost bounds, not as tight bounds. Yet in many cases this strategy results in a simple design procedure and a nearly optimal outcome. Second, if the targeting model is exact, as in Pinch Analysis for Heat Integration (Linnhoff and Flower, 1978), or if it at least captures all key factors at the corresponding design stage, as with Regional Energy Clustering (Lam, Varbanov, and Klemeš, 2010), then the targeting procedure also provides a convenient partitioning of the original design space. This makes it easier to decompose the problem and to simplify the remaining actions. A good example of partitioning the design space is the division above/below the Pinch in Heat Integration (see Chapter 4).

3.10.6 Handling Model Nonlinearity As discussed in Section 3.5, convex problems are guaranteed to produce globally optimal results when solved with deterministic algorithms that employ local search. In contrast, a nonconvex optimization problem is difficult to solve, and its solution is not guaranteed to be a global optimum. All linear MP models are convex (Williams, 1999). With nonlinear models, however, the problem convexity must be established on a case-by-case basis. Nonlinear models hinder the computation process of the solvers (e.g., by requiring that feasible initial solutions be provided), and they often result in poor numerical convergence. This is why engineers usually seek ways to obtain linear models in some form. Crucial factors in this task are preserving the model’s precision and validity.

Trading Off Precision and Linearization Sometimes it is possible to linearize relationships that are inherently nonlinear. This can be done, for instance, by replacing a single nonlinear relationship with two or more linear ones that, together, approximate the original function over the required range. This technique is known as piecewise linearization. For example, it can be applied when the available cost functions (for piping, distillation columns, or heat exchangers) are too complex. The result of this approach is a small reduction in the overall model precision and an increase in the number of integer variables in the model; thus, combinatorial complexity is increased but computational complexity (due to nonlinearity) is reduced. The principal advantage is the resulting linearity of the model, which almost always makes it easier to solve than the original one. Caution must be exercised in the process of linearization: the loss of precision must be kept as small as

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Chapter Three possible so that the resulting model remains an adequate representation of the underlying process. Another pitfall is a potentially unacceptable increase in combinatorial complexity, which can result if too many linear segments are used to approximate the original relationship.

Discretization of Continuous Process Variables Another approach to avoiding nonlinearity is to define a number of fixed levels for some variables and then to substitute the original nonlinear variables in the model with linear combinations of integer variables and parameters (where the parameters are derived from the original variables). In this way, the bilinear terms in the mass balances of contaminants can be reduced to purely linear expressions. In its consequences and pitfalls, this technique is similar to piecewise linearization.

Other Techniques There are other approaches and techniques for coping with nonlinear models. Two of them are of particular interest to practical process optimization: successive MILP (SMILP), which is used for model decomposition and solving; and model reformulation. Successive MILP can be applied to many process engineering optimization models—as long as the nonlinearities are not too strong. One example is the optimization of utility systems, which consist mainly of a set of steam headers combined with steam turbines, gas turbines, boilers, and letdowns. Most of the nonlinearities in such systems are bound to the enthalpy balances of the steam headers, the steam turbines, and the letdowns. The computational difficulties imposed by the nonlinearities can be overcome by first fixing the values of some system properties during optimization (e.g., enthalpies of steam mains), thereby producing a linear optimization model, and following this with a rigorous simulation after each optimization step. The linear optimization steps are repeated, followed again by simulation, and so on until convergence is achieved; see Figure 3.2. This procedure converges rapidly when applied to the optimization of existing utility systems: usually five iterations at most are required to reach reasonably small error levels. Model reformulation refers to the symbolic transformation of the original nonlinear equations into another set of equations that are equivalent but linear. The resulting set usually contains more equations than the initial one. One such reformulation technique, known as the Glover transformation (Floudas 1995), can transform equations containing the product of a continuous and a binary variable. The essence of the technique is to replace each term that is a product of a continuous variable and a binary variable with additional continuous variables and an additional set of linear inequality constraints.

Process Optimization BEGIN Initialization (+Simulation)

MILP

Convergence?

Simulation

NO

YES END

FIGURE 3.2

3.10.7

SMILP procedure for solving nonlinear optimization problems.

Evaluating Model Adequacy and Precision

Once the model is built, the next step is validation. This process boils down to evaluating how precisely the model predicts real-life phenomena as well as how adequately it represents the modeled system (Steppan, Werner, and Yeater, 1998; Montgomery, 2005). If the model turns out to be imprecise or inadequate, then the reasons for these shortcomings must be discovered and addressed. This iterative process is similar to debugging during software development. It is generally accepted that residuals (and their plots) are sufficient for assessing whether a given model accurately predicts the underlying process. The residual plots can be used to minimize or even eliminate stochastic errors. In addition, parity plots are helpful in exposing any systematic errors in the model. The final check is to analyze the model’s variance (Steppan, Werner, Yeater, 1998; Montgomery, 2005). In essence, this means determining whether the empirically derived coefficients and the model’s predictions have any statistical significance. This is performed by means of a standard procedure for the “Analysis of Variance” (ANOVA).

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CHAPTER

4

Process Integration for Improving Energy Efficiency

H

eat recovery is widely applied in industrial processes and has an extensive historical record. However, systematic methods for performing heat recovery are relatively new when compared with the age of modern industry.

4.1 Introduction to Heat Exchange and Heat Recovery In industry, large amounts of thermal energy are used to perform heating. Examples of this can be found in crude oil preheating before distillation, preheating of feed flows to chemical reactors, and heat addition to carry out endothermic chemical reactions. Similarly, some processes—such as condensation, exothermal chemical reactions, and product finalization—require that heat be extracted, which results in process cooling. There are several options for utility heating; these include steam, hot mineral oils, and direct fired heating. Steam is the most prevalent option because of its high specific heating value in the form of latent heat. Utility cooling options include water (used for moderate-temperature cooling when water is available), air (used when water is scarce or not economical to use), and refrigeration (when subambient cooling is needed). Heat recovery can be used to provide either heating or cooling to processes. Heat recovery may take various forms: transferring heat between process streams, generating steam from higher-temperature process waste heat, and preheating (e.g., air for a furnace, air or feed water for a boiler using waste heat). Heat transfer takes place in heat exchangers, which can employ either direct mixing or indirect heat transfer via a wall. Direct heat exchange is also referred to as nonisothermal mixing because the temperatures of the mixed streams are different. Mixing heat exchangers are efficient at transferring heat and usually have low

45

46

Chapter Four capital cost. In most industries, the bulk of the heat exchange must occur without mixing the heat-exchanging streams. In order to exchange only heat while keeping the streams separate, surface heat exchangers are employed. In these devices, heat is exchanged through a dividing wall. Because of its high thermal efficiency, the countercurrent stream arrangement is the most common with surface heat exchangers. To simplify the discussion, counter-current heat exchangers are assumed unless stated otherwise. In terms of construction types, the traditional shell-and-tube heat exchanger is still the most common. However, plate-type and other compact heat exchangers are gaining increased attention. Their compactness, together with significant improvements in their resistance to leaking, have made them preferable in many cases.

4.1.1 Heat Exchange Matches A hot process stream can supply heat to a cold one when paired in one or several physical heat exchangers arranged in parallel or sequence. Each such pairing is referred to as a heat exchange match. The form of the steady-state balance equations for heat exchange matches that is most convenient for Heat Integration calculations is based on modeling a match as consisting of hot and cold sides, as shown in Figure 4.1. The hot and cold part each have a simple, steadystate enthalpy balance that involves just one material stream and one heat transfer flow. The main components of the model are (1) calculations of the heat transfer flows accounted for by the enthalpy balances and (2) estimation of the necessary heat transfer area. For the latter, both the log-mean temperature difference and the overall heat transfer coefficient are employed. The enthalpy balance of the hot and cold parts, and the kinetic equation of the heat transfer, may be written as follows: QHE

mhot ˜  hin,hot  hout,hot

(4.1)

Hot part hIN,HOT

hOUT,HOT mHOT

mHOT

QHE hIN,COLD

mCOLD

hOUT,COLD mCOLD

Cold part

FIGURE 4.1

Process flow diagram of a heat exchange match.

Process Integration for Improving Energy Efficiency QHE

mcold ˜  hout,cold  hin,cold

(4.2)

QHE

U ˜ A ˜ ⌬TLM

(4.3)

where QHE [kW] is the heat flow across the whole heat exchanger, U [kW∙m−2∙°C−1] is the overall heat transfer coefficient, A [m2] is the heat transfer area, and ΔTLM [°C] is the logarithmic-mean temperature difference. More information can be found in Shah and Sekulić (2003), Tovazshnyansky et al. (2004), and Shilling et al. (2008).

4.1.2 Implementing Heat Exchange Matches The heat exchange matches are often viewed as being identical to heat exchangers, but this is not always the case. A given heat exchange match may be implemented by devices of different construction or by a combination of devices—for example, two heat exchangers in sequence may implement a single heat exchange match. The distinction between the concept of a heat exchange match and its implementation via heat exchangers is important because of capital cost considerations.

4.2 Basics of Process Integration 4.2.1 Process Integration and Heat Integration A historical review of the field was given in Chapter 2. Initially, attention was focused on reusing any waste heat generated on different sites. Each surface heat exchanger was described with only a few steady-state equations, and the thermal energy saved by reusing waste heat led to reductions in the expense of utility resources. This approach became popular under the names Heat Integration (HI) and the more general term Process Integration (PI). In this context, HI means integrating different processes to achieve energy savings. Engineers realized that integration could also reduce the consumption of other resources as well as the emission of pollutants. Heat and Process Integration came to be defined more widely in response to similar developments in water reuse and wastewater minimization.

4.2.2 Hierarchy of Process Design Process design has an inherent hierarchy that can be exploited for making design decisions. This hierarchy may be represented by the so-called onion diagram (Linnhoff et al., 1982), as shown in Figure 4.2. The design of an industrial process starts with the reactors or other key operating units (the onion’s core). This is supplemented and served by other parts of the process, such as the separation subsystem (the next layer) and the Heat Exchanger Network (HEN) subsystem.

47

Chapter Four

Ambient Utilities

Reactor

He a

tE

ng xcha er Ne t arato p e r S

rk wo

Feed

Separator

48

Reactor

Feed + Product

Product

Steam Turbine Boiler

FIGURE 4.2

The onion diagram.

The remaining heating and cooling duties, as well as the power demands, are handled by the utility system.

4.2.3 Performance Targets The thermodynamic bounds on heat exchange can be used to estimate the utility usage and heat exchange area for a given heat recovery problem. The resulting estimates of the process performance are a lower bound on the utility demands and a lower bound on the required heat transfer area. These bounds are known as targets for the reason that heat recovery estimates are achievable in practice and usually minimize the total cost of the HEN being designed.

4.2.4 Heat Recovery Problem Identification For efficient heat recovery in industry, the relevant data must be identified and presented systematically. In the field of Heat Integration, this process is referred to as data extraction. The heat recovery problem data are extracted in several steps: 1. Inspect the general process flowsheet, which may contain heat recovery exchangers. 2. Remove the recovery heat exchangers and replace them with equivalent “virtual” heaters and coolers. 3. Lump all consecutive heaters and coolers. 4. The resulting virtual heaters and coolers represent the net heating and cooling demands of the flowsheet streams. 5. The heating and cooling demands of the flowsheet streams are then listed in a tabular format, where each heating

Process Integration for Improving Energy Efficiency demand is referred to as a cold stream and, conversely, each cooling demand as a hot stream. This procedure is best illustrated by an example. Figure 4.3 shows a process flowsheet involving two reactors and a distillation column. The process already incorporates two recovery heat exchangers. The utility heating demand of the process is H = 1760 kW, and the utility cooling demand is C = 920 kW. The necessary thermal data has to be extracted from the initial flowsheet. Figure 4.4 shows the flowsheet after steps 1 through 4. The heating and cooling demands of the streams have been consolidated by removing the existing exchangers, and the reboiler and condenser duties have been left out of the analysis for simplicity (although these duties would be retained in an actual study). It is assumed that any process cooling duty is available to match up with any heating duty. Applying step 5 to the data in Figure 4.4 produces the data set in Table 4.1. By convention, heating duties are positive and cooling ones are negative. (The subscripts S and T denote “supply” and “target” temperatures for the process streams.) The last column of Table 4.1 gives the heat capacity flow rate (CP). For streams that do not change phase (i.e., from liquid to gas or vice versa), CP is defined as the product of the specific heat capacity and the mass flow rate of the corresponding stream: mstream ˜ Cp ,stream

CP

(4.4)

Condenser

Column

52°C 2080 kW

78°C

182°C Reactor 2

1760 kW H 138°C

120°C Reactor 1

Reboiler 100°C

120°C 3240 kW

920 kW C

FIGURE 4.3 2005).

30°C 34°C

Data extraction: Example process flowsheet (after CPI, 2004 and

49

50

Chapter Four

Condenser

Column

52°C 78°C

Cooling 2080 kW

Reactor 2 Heating 3840 kW

138°C

182°C

120°C Reactor 1

Reboiler 100°C

Cooling 4160 kW

120°C Heating 3240 kW

34°C

30°C

FIGURE 4.4 Data extraction: Heating and cooling demands (after CPI, 2004 and 2005).

Stream

Type

T S [°C]

T T [°C]

ΔH [kW]

CP [kW/°C]

H1

Hot

182

78

−2080

20

H2

Hot

138

34

−4160

40

C3

Cold

52

100

3840

80

C4

Cold

30

120

3240

36

TABLE 4.1

Data Set for Heat Recovery Analysis

The CP can also be calculated using the following simple equation: CP

⌬H TT  TS

⌬H ⌬T

(4.5)

When phase transition occurs, the latent heat is used instead of CP to calculate the stream duties. Some more problems related to data extraction are discussed in Chapter 12.

4.3 Basic Pinch Technology The main strategy of Pinch-based Process Integration is to identify the performance targets before starting the core process design activity. Following this strategy yields important clues and design guidelines. The most common hot utility is steam. Heating with steam is usually approximated as a constant-temperature heating

Process Integration for Improving Energy Efficiency utility. Cooling with water is nonisothermal because the cooling effect results from sensible heat absorption into the water stream and thus leads to increasing the temperature.

4.3.1 Setting Energy Targets Heat Recovery between One Hot and One Cold Stream The Second Law of thermodynamics states that heat flows from higher-temperature to lower-temperature regions. As shown in Eq. (4.3), in a heat exchanger the required heat transfer area is proportional to the temperature difference between the streams. In HEN design, the minimum allowed temperature difference (ΔTmin) is the lower bound on any temperature difference to be encountered in any heat exchanger in the network. The value of ΔTmin is a design parameter determined by exploring the trade-offs between more heat recovery and the larger heat transfer area requirement. Any given pair of hot and cold process streams may exchange as much heat as allowed by their temperatures and the minimum temperature difference. Consider the two-stream example shown in Figure 4.5(a). The amount of heat recovery is 10 MW, which is achieved by allowing ΔTmin = 20°C. If ΔTmin = 10°C, as in Figure 4.5(b), then it is possible to “squeeze out” one more megawatt of heat recovery. To obtain the heat recovery targets for a practical HEN design problem, this principle needs to be extended to handle multiple streams.

Evaluation of Heat Recovery for Multiple Streams: The Composite Curves The analysis starts by combining all hot streams and all cold streams into two Composite Curves or CCs (Linnhoff et al., 1982). For each process there are two curves: one for the hot streams (Hot Composite Curve, HCC) and another for the cold streams (Cold Composite Curve, CCC). Each Composite Curve (CC) consists of a (a) T [°C] 200

(b) T [°C] 200

Steam

150

150

100

100 50

20°C

50

Steam

10°C

CW 0 2

CW 10 10

4

20 ΔH [MW]

Heat recovery at ΔTMIN = 20°C

FIGURE 4.5

0 1

10 11

3

20 ΔH [MW]

Heat recovery at ΔTMIN = 10°C

Thermodynamic limits on heat recovery.

51

Chapter Four temperature-enthalpy (T-H) profile, representing the overall heat availability in the process (the HCC) and the overall heat demands of the process (the CCC). The procedure of HCC construction is illustrated in Figure 4.6 on the data from Table 4.1. All temperature intervals are formed by the starting and target temperatures of the hot process streams. Within each temperature interval, a composite segment is formed consisting of (1) a temperature difference equal to that of the interval and (2) a total cooling requirement equal to the sum of the cooling requirements of all streams within the interval. This is achieved by summing up the heat capacity flow rates of the streams crossing the interval. Next, the composite segments from all temperature intervals are combined to form the HCC. Construction of the CCC is entirely analogous. The Composite Curves are combined in the same graph in order to identify the maximum overlap, which represents the maximum amount of heat that could be recovered. The HCC and CCC for the example from Table 4.1 are shown together in Figure 4.7. Both CCs can be moved horizontally (i.e., along the ΔH axis), but usually the HCC position is fixed and the CCC is shifted. This is equivalent to varying the amount of heat recovery and (simultaneously) the amount of required utility heating and cooling. Where the curves overlap, heat can be recuperated between the hot and cold streams. More overlap means more heat recovery and smaller utility requirements, and vice versa. As the overlap increases, the temperature differences between the overlapping curve segments decrease. Finally, at a certain overlap, the curves reach the minimum allowed temperature difference, ΔTmin. Beyond this point, no further overlap is possible. The closest approach between the curves is termed the Pinch point (or simply the Pinch); it is also known as the heat recovery Pinch. It is important to note that the amount of largest overlap (and thus the maximum heat recovery) would be different if the minimum

(a) T [°C]

(b) T [°C] /°C

CP2 = 40 kW/°C

20

138

=

78

CP

2

=4

78 34

34 2080

4160 6240

ΔH [kW]

The hot streams plotted separately

FIGURE 4.6

= P2 +C C CP 1 kW/° 60

/°C

W 0k

1

138

182

kW

182

CP

52

CP1 = 20 kW/°C

3600 880 ΔH [kW] 6240 The composite hot stream

1760

Constructing the Hot Composite Curve.

Process Integration for Improving Energy Efficiency allowed temperature difference is changed for the same set of hot and cold streams. The larger is the value of ΔTmin, the smaller is the possible maximum heat recovery. Specifying the minimum utility heating, the minimum utility cooling, or the minimum temperature difference fixes the relative position of the two Composite Curves and hence the maximum possible amount of heat recovery. The identified heat recovery targets are not absolute—they are relative to the specified value of ΔTmin. If that value is increased, then the minimum utility requirements also increase and the potential for maximum recovery drops; see Figure 4.8. T [°C] 200

150

Pinch

100

50 ΔTmin = 10°C 0 Qc,min = 328

FIGURE 4.7

Qrec = 5912

Qh,min = 1168

ΔH [kW]

The HCC and CCC at ΔTmin = 10°C.

T [°C] 200

150 Pinch 100

ΔTmin = 10°C

50 ΔTmin = 20°C 0 Qc,min = 328

Qrec = 5912

Qh,min = 1168

Qc,min = 728

Qrec = 5512

Qh,min = 1568

FIGURE 4.8

Variation of heat recovery targets with ΔTmin.

ΔH [kW]

53

54

Chapter Four The appropriate value for ΔTmin is determined by economic tradeoffs. Increasing ΔTmin results in larger minimum utility demands and increased energy costs; choosing a higher value reflects the need to reduce heat transfer area and its corresponding investment cost. Conversely, if ΔTmin is reduced then utility costs go down but investment costs go up. This trade-off is illustrated in Figure 4.9.

4.3.2 The Heat Recovery Pinch The heat recovery Pinch has important implications for the HEN being designed. As illustrated in Figure 4.10, the Pinch sets the absolute limits for heat recovery within the process. COST

Total

Energy

Capital 1

2 ΔTMIN

Optimum

FIGURE 4.9 ΔTmin.

Trade-off between investment and energy costs as a function of

T

QH,min

PINCH

Qc,min ΔH

FIGURE 4.10

Limits for process heat recovery set by the Pinch.

Process Integration for Improving Energy Efficiency The Pinch point divides the heat recovery problem into a net heat sink above the Pinch point and a net heat source below it (Figure 4.11). At the Pinch point, the temperature difference between the hot and cold streams is exactly equal to ΔTmin, which means that at this point the streams are not allowed to exchange heat. As a result, the heat sink above the Pinch is in balance with the minimum hot utility (QH,min) and the heat source below the Pinch is in balance with the minimum cold utility (QC,min), while no heat is transferred across the Pinch via utilities or via process-to-process heat transfer. No heat can be transferred from below to above the Pinch, because this is thermodynamically infeasible. However, it is feasible to transfer heat from hot streams above the Pinch to cold streams below the Pinch. All cold streams—even those below the Pinch— could be heated by a hot utility; likewise, the hot streams (even above the Pinch) could be cooled by a cold utility. Although these arrangements are thermodynamically feasible, applying them would cause utility use to exceed the minimum, as identified by the Pinch Analysis. This is a fundamental relationship in the design of heat recovery systems. What happens if heat is transferred across the Pinch? Recall that it is possible to transfer heat only from above to below the Pinch. If, say, XP units of heat are transferred across the Pinch (Figure 4.12), then QH,min and QC,min will each increase by the same amount in order to maintain the heat balances of the two problem parts. Any extra heat that is added to the system by the hot utility must then be taken away by the cold utility, in addition to the minimum requirement QC,min. Cross-Pinch process-to-process heat transfer is not the only way by which a problem’s thermodynamic Pinch partitioning can be

T Zero crosspinch transfer

ΔTmin

QH,min

Pinch

QC,min ΔH

FIGURE 4.11

Partitioning the heat recovery problem.

55

56

Chapter Four T

QH,min QUC,above

QUH,below

XP

XP

PINCH

XP

FIGURE 4.12

QUH,below

QC,min

QUC,above

ΔH

More in, more out.

violated. This could also happen if the external utilities are placed incorrectly. For example, any utility heating below the Pinch will create a need for additional utility cooling in that part of the system (Figure 4.12). Conversely, any utility cooling above the Pinch will create a need for additional utility heating. The implications of the Pinch for heat recovery problems can be distilled into the following three conditions, which must hold if the minimum energy targets for a process are to be achieved. 1. Heat must not be transferred across the Pinch. 2. There must be no external cooling above the Pinch. 3. There must be no external heating below the Pinch. Violating any of these rules will lead to an increase in energy utility demands. The rules are applied explicitly in the context of HEN synthesis by the Pinch Design Method (Linnhoff and Hindmarsh, 1983) and also before a HEN retrofit analysis to identify causes of excessive utility demands by a process. Other HEN synthesis methods—if they achieve the minimum utility demands—also conform to the Pinch rules (though sometimes only implicitly).

4.3.3 Numerical Targeting: The Problem Table Algorithm The Composite Curves are a useful tool for visualizing heat recovery targets. However, they can be time-consuming to draw for problems that involve many process streams. In addition, targeting that relies solely on such graphical techniques cannot be very precise. The process of identifying numerical targets is therefore usually based on an algorithm known as the Problem Table Algorithm (PTA). Some

Process Integration for Improving Energy Efficiency MPR-oriented authors employ the equivalent “transshipment” model (Cerdá et al., 1990). The steps are as follows: 1. Shift the process stream temperatures. 2. Set up temperature intervals. 3. Calculate interval heat balances. 4. Assuming zero hot utility, cascade the balances as heat flows. 5. Ensure positive heat flows by increasing the hot utility as needed. The algorithm will be illustrated using the sample data in Table 4.2.

Step 1 Because the PTA uses temperature intervals, it is necessary to set up a unified temperature scale for the calculations. If the real stream temperatures are used, then some of the heat content would be left out of the recovery. The problem is avoided by obtaining shifted stream temperatures (T*) for PTA calculations. The hot streams are shifted to be colder by ΔTmin/2 and the cold streams are shifted to be hotter by ΔTmin/2. If the shifted temperatures (T*) of a cold and a hot stream (or their parts) are the same, then their real temperatures are still actually ΔTmin apart, which allows for feasible heat transfer. This operation is equivalent to shifting the Composite Curves toward each other vertically, as illustrated in Figure 4.13. The last two columns in Table 4.2 show the shifted process stream temperatures.

Step 2 Temperature intervals are formed by listing all shifted process stream temperatures in descending order (any duplicate values are Shifter Composite Curves T* T 2

T

Cold

−

ΔTmin

Hot

Temperature

T*

+

ΔTmin 2

ΔH

FIGURE 4.13

Temperature shifting to ensure feasible heat transfer.

57

58

Chapter Four No.

Type

T S [°C]

T T [°C]

1

Cold

2

Hot

250

40

15

245

35

3

Cold

140

230

30

145

235

4

Hot

200

80

25

195

75

20

CP [kW/°C]

180

20

T S*[°C] 25

T T*[°C] 185

TABLE 4.2 Problem Table Algorithm Example: Process Streams Data (ΔTmin = 10°C) Interval Temp. [oC]

Stream Population

∑ CPH −∑ CPC [kW/oC]

∆Hinterval [kW]

10

15

150

Surplus

40

−15

600

Deficit

10

10

−100

Surplus

40

−10

−400

Deficit

70

20

1400

Surplus

40

−5

−200

Deficit

10

20

−200

Deficit

∆Tinterval [oC]

Surplus/ Deficit

2

245 235

4

145 CP = 20

3

75

35 25

CP = 25

CP = 15

185

CP = 30

195

1

TABLE 4.3

Problem Table Algorithm for the Streams in Table 4.2

considered just once). This action creates temperature boundaries (TBs), which form the temperature intervals for the problem. For the example in Table 4.2, the TBs are 245°C, 235°C, 195°C, 185°C, 145°C, 75°C, 35°C, and 25°C.

Step 3 The heat balance is calculated for each temperature interval. First, the stream population of the process segments falling within each temperature interval (the first two columns of Table 4.3) is identified.

Process Integration for Improving Energy Efficiency Next, the sums of the segment CPs (heat capacity flow rates) in each interval are calculated; then that sum is multiplied by the interval temperature difference (i.e., the difference between the TBs that define each interval). This calculation is also illustrated in Table 4.3.

Step 4 The Problem Heat Cascade shown in Figure 4.14 has a box allocated to each temperature interval; each box contains the corresponding interval enthalpy balances. The boxes are connected with heat flow arrows in order of descending temperature. The top heat flow represents the total hot utility provided to the cascade, and the bottom heat flow represents the total cold utility. The hot utility flow is initially assumed to be zero and this value is combined (summed) with the enthalpy balance of the top cascade interval to produce the value for the next lower cascade heat flow. This operation is repeated for the lower temperature intervals and connecting heat flows until the bottom heat flow is calculated, resulting in the cascade shown in Figure 4.14(a).

Step 5 The resulting heat flow values in the cascade are examined, and a feasible heat cascade is obtained; see Figure 4.14(b). From the cascading heat flows, the smallest value is identified; if it is nonnegative (i.e., positive or zero), then the heat cascade is thermodynamically feasible. If a negative value is obtained then a positive utility flow of the same absolute value has to be provided at

HOT UTILITY (b)

(a) 245 °C

0 kW

HOT UTILITY

245 °C ΔH = 150 kW

ΔH = 150 kW

235 °C

150 kW ΔH = −600 kW

235 °C 195 °C

−350 kW −750 kW −650 kW −450 kW

250 kW HOT UTILITY (a) Initial cascade

FIGURE 4.14

* TPINCH 0 kW

75 °C

THOT PINCH = 150°C TCOLD PINCH = 140°C

1400 kW

35 °C

1200 kW

ΔH = −200 kW

ΔH = −200 kW

25 °C

145 °C

ΔH = −200 kW

ΔH = −200 kW

35 °C

400 kW

ΔH = 1400 kW

ΔH = 1400 kW

75 °C

185 °C ΔH = −400 kW

ΔH = −400 kW

145 °C

300 kW ΔH = 100 kW

ΔH = 100 kW

185 °C

900 kW

ΔH = −600 kW

−450 kW

195 °C

750 kW

25 °C

1000 kW HOT UTILITY

(b) Feasible cascade

Heat Cascade for the process data in Table 4.2.

59

60

Chapter Four the topmost heat flow, after which the cascading described in Step 4 is repeated. The resulting heat cascade is guaranteed to be feasible and provides numerical heat recovery targets for the problem. The topmost heat flow represents the minimum hot utility, the bottommost heat flow represents the minimum cold utility, and the TB with zero heat flow represents the location of the (heat recovery) Pinch. It is often possible to obtain more than one zero-flow temperature boundary, each representing a separate Pinch point.

4.3.4

Threshold Problems

Threshold problems feature only one utility type—either hot or cold. They are important mostly because they often result in no utility– capital trade-off below a certain value of ΔTmin, since the minimum utility demand (hot or cold) becomes invariant; see Figure 4.15. (a) T

(b) T

Steam

ΔTmin = 14°C

ΔTmin = 20°C

CW

CW ΔH

More heat recovery, no hot utility

Heat recovery, hot and cold utilities

ΔH

(d) T

(c) T

ΔTmin = 10°C

ΔTmin = 10°C

CW

CW ΔH

No increase in heat recovery

FIGURE 4.15

Steam Generation

CW

Utility substitution

ΔH

Threshold HEN design cases.

Typical examples of threshold Heat Integration problems involve high-temperature fuel cells, which usually have large net cooling demands but no net heating demands (Varbanov et al., 2006; Varbanov and Klemeš, 2008). An essential feature that distinguishes threshold problems is that, as ΔTmin is varied, demands for only one

Process Integration for Improving Energy Efficiency utility type (hot or cold) are identified over the variation range; in contrast, pinched problems require both hot and cold utilities over this range. When synthesizing HENs for threshold problems, one can distinguish between two subtypes (see Figure 4.16): 1. Low-threshold ΔTmin: Problems of this type should be treated exactly as Pinch-type problems. 2. High-threshold ΔTmin: For these problems, it is first necessary to satisfy the required temperature for the no-utility end before proceeding with the remaining design (using the tickoff heuristic; see Figure 4.53).

4.3.5 Multiple Utilities Targeting Utility Placement: Grand Composite Curve In many cases, more than one hot and one cold utility are available for providing the external heating and cooling requirements after energy recovery and it is necessary to find and evaluate the (a)

T

ST

Utilities [MW] CW ST

10°C

ΔTmin = 10°C

ΔTmin

CW ΔH [MW]

Low Threshold ΔTmin T

(b)

ST

Utilities [MW]

ST CW

10°C

ΔTmin High Threshold ΔTmin

FIGURE 4.16

Threshold problems.

ΔTmin = 10°C ΔH [MW]

61

62

Chapter Four cheapest and most effective combination of the available utilities (Figure 4.17). To assist with this choice and to enhance the information derived from the HCC and CCC, another graphical construction has been developed, known as the Grand Composite Curve (GCC) (Townsend and Linnhoff, 1983). The heat cascade and the PTA (Linnhoff and Flower, 1978) offer guidelines for the optimum placement of hot and cold utilities, and this allows one to determine the heat loads associated with each utility. For the previous sections, the assumption has been that only one cold and one hot utility are available—albeit with sufficiently low and high temperatures to satisfy the cooling and/or heating demands of the process. However, most industrial sites feature multiple heating and cooling utilities at several different temperature levels (e.g., steam levels, refrigeration levels, hot oil circuit, furnace flue gas). Each utility has a different unit cost. Usually the higher-temperature hot utilities and the lower-temperature cold utilities cost more than the ones with temperatures closer to the ambient. This fact underscores the need to choose a mix that results in the lowest utility cost. The general objective is to maximize the use of cheaper utilities and to minimize the use of more expensive utilities. For example, it is usually preferable to use low-pressure (LP) instead of high-pressure (HP) steam and to use cooling water (CW) instead of refrigeration. The Composite Curves plot in Figure 4.7 provides a convenient view for evaluating the process driving force and the general heat recovery targets. However, the CCs are not useful for identifying targets when multiple utility levels are available; the GCC is used for this task.

Boiler House and Power Plant Fuel

Fuel

HP

Steam Levels

Power MP

Steam turbine

LP BFW preheat

Heating Heating

Power

Gas turbine

Heating

Heating

Heating (Q+W)

Processes, building complexes

Heat pump

Heating Cooling

Refrigeration

Furnace Fuel

FIGURE 4.17 2005).

Cooling

Air preheat

Heating

Cooling (Q)

Power (W)

Power

Choices of hot and cold utilities (amended after CPI 2004 and

Process Integration for Improving Energy Efficiency

Construction of the Grand Composite Curve The GCC is constructed using the Problem Heat Cascade (Figure 4.14). The heat flows are plotted in the T-ΔH space, where the heat flow at each temperature boundary corresponds to the X coordinate and the temperature to the Y coordinate (Figure 4.18). The GCC can be directly related to the Shifted Composite Curves (SCCs), which are the result of shifting the CCs toward each other by ΔTmin/2 so that the curves touch each other at the Pinch; see Figure 4.19. At each temperature boundary, the heat flow in the Problem Heat Cascade and GCC corresponds to the horizontal distance between the SCCs. The GCC has several fundamental properties that facilitate an understanding of the underlying heat recovery problem. The parts with positive slope (i.e., running uphill from left to right) indicate that cold streams dominate (Figures 4.18 and 4.19). Similarly, the parts with negative slope indicate excess hot streams. The shaded areas in the GCC plot, which signify opportunities for process-toprocess heat recovery, are referred to as heat recovery pockets.

Utility Placement Options The GCC shows the hot and cold utility requirements of the process in terms of both enthalpy and temperature. This allows one to distinguish between utilities at different temperature levels. There are typically

T* (°C)

Hot Utility

ΔH= 150 kW

750 kW 245 °C 900 kW 235 °C

ΔH= 600 kW

ΔH= 100 kW ΔH= 400 kW

300 kW 195 °C 400 kW 185 °C 0 kW

PINCH

145 °C ΔH= 1400 kW 1400 °C 75 °C ΔH= −200 kW 1200 kW ΔH= −200 kW

35 °C 1000 kW 25 °C

Cold Utility 500

1000

1500 Q (kW)

FIGURE 4.18

Constructing the GCC for the streams in Table 4.2.

63

64

Chapter Four T* [°C]

T* [°C]

300

300 750

750 200

900

300

900 200

300 400

400

100

100

1400 1200

1400 1200

1000

1000

0

500

1000

1500

0

2000

4000

6000

8000

ΔH [kW]

Q [kW]

FIGURE 4.19 Relation between the GCC (left) and the SCC (right) for the streams in Table 4.2.

(a) T* [°C]

(b) T* [°C] HP steam

HP steam 200 MP steam

200 PINCH

PINCH

100

100

Cooling Water

Cooling Water 0

500

1000

Single steam level

FIGURE 4.20

Q [kW]

Q [kW] 1500

0

500

1000

1500

Multiple steam levels

Using the GCC to target for single and multiple steam levels.

utilities at several different temperature levels available on a site—for example, there may be a supply of both high-pressure (HP) and medium-pressure (MP) steam. As indicated previously, it is desirable to maximize the use of cheaper utilities and to minimize the use of more expensive ones. Utilities at higher temperature and/or pressure are usually more expensive; see Figure 4.20. Therefore, MP steam is used first: ranging from the Y axis until it touches the GCC (resulting in ΔTmin in this point), which maximizes its usage. Only then is HP steam used. When a utility line or profile touches the GCC, a new Pinch point is created, termed a Utility Pinch (the MP steam line touching the GCC in Figure 4.20). Each additional steam level creates another Utility Pinch and increases the complexity of the utility system.

Process Integration for Improving Energy Efficiency Higher complexity has several negative consequences, including increased capital costs, greater potential for leaks, reduced safety, and more maintenance expenses. Therefore limits are typically placed on the number of steam levels. Higher-temperature heating demands are satisfied by nonisothermal utilities. These include hot oil and hot flue gas, both of which maintain their physical phase (liquid and gaseous) across a wide range of temperatures. The operating costs associated with such utilities are largely dependent on furnace efficiency and on the intensity and efficiency of the pumping or fan blowing. When targeting the placement of a nonisothermal hot utility, its profile is represented by a straight line,1 which runs from the upper right to the lower left in the graph of Figure 4.21. The line’s starting point corresponds to the utility supply temperature and also to the rightmost point for the utility’s heating duty. The utility use endpoint corresponds either to the zero of the ΔH axis—in which case all utility heating is covered by the current nonisothermal utility—or to the rightmost point on the ΔH axis for other, cheaper hot utilities.

T*

FIGURE 4.21 Properties of nonisothermal hot utilities.

* Tsupply

CP1 CP2

CP1 > CP2

T*ambient ΔHloss,2 ΔHloss,1

ΔH

1 This linear representation assumes an approximately constant specific heat capacity of the corresponding stream.

65

Chapter Four As plotted in the figure, the nonisothermal utility’s termination point corresponds to the ambient temperature. The distance from this point to the zero of the ΔH axis represents the thermal losses from using the utility. The heat capacity flow rate of the nonisothermal utility target is determined by making the utility line as steep as possible, thereby minimizing its CP and the corresponding losses (Figure 4.21). Its supply temperature is usually fixed at the maximum allowed by the furnace and the heat carrier composition; the remaining degree of freedom corresponds to the utility’s exact CP. Smaller CP values result in steeper slopes and smaller losses. The placement for a nonisothermal utility (e.g., hot oil) may be constrained by two problem features: the process Pinch point and a “kink” in the GCC at the top end of a heat recovery pocket; see Figure 4.22 for an example. When fuel is burned in a furnace or a boiler, the resulting flue gas becomes available to heat up the corresponding cold-stream medium (for steam generation or direct process duty). Transferring heat to the process causes the flue gas temperature to drop as it moves from the furnace to the stack. The stack temperature has to be above a specified value: the minimum allowed stack temperature, which is determined by limitations due to corrosion. If flue gas is used directly for heating, then the Pinch point, if it is higher, may become more limiting than the minimum allowed stack temperature. If the analyzed process features both high-temperature and moderatetemperature utility heating demands, then flue gas heating may not be appropriate for satisfying all those demands. If steam is cheaper,

ΔTmin= 20

(a) T*

(b) * T 290

290

Minimizing the CP

Tsupply = 300 Minimizing the CP

in

CP

mi

n

The Pinch does not need to be limiting

TReturn, min =130

CP m

66

TReturn, min= 150 Pinch

120

120

Pinch ΔH

ΔH Process Pinch limitation

FIGURE 4.22

Heat recovery pocket limitation

Constraints for placing hot oil utilities, ΔTmin = 20 °C.

Process Integration for Improving Energy Efficiency then combining it with flue gas reduces the latter’s CP and the corresponding stack heat losses. Another option for utility placement is to use part of the cooling demand of a process for generating steam. This is illustrated in Figure 4.23, in which steam generation is placed below the Pinch. The GCC can reveal where utility substitution may improve energy efficiency; see Figure 4.24. The main idea is to exploit heat recovery pockets that span two or more utility temperature levels. The technical feasibility of this approach is determined by both the temperature span and the heat duty within the pocket, which should be large enough to make utility substitution worthwhile when weighed against the required capital costs. Utility cooling below ambient temperatures may be required, a need that is usually met by refrigeration. Refrigerants absorb heat by evaporation, and pure refrigerants evaporate at a constant temperature. Therefore, refrigerants are represented—on the plot of T (or T*) versus ΔH—by horizontal bars, similarly to the steam levels. On the GCC, refrigeration levels are placed similarly to steam levels; see Figure 4.25. When the level of a placed utility is between the temperatures of a heat recovery pocket, the Utility Pinch cannot be located by using

Pinch

T*

160

140 Point of closest approach. Not necessarily at the boiling point

120

100 Preheat Evaporation

Superheat 80

60

40

Cooling Water QC,min

20 0

FIGURE 4.23

Generating steam below the Pinch.

ΔH

67

68

Chapter Four T*

T*

HP Steam Generation

HP Steam Generation

LP Steam use

CW

CW ΔH

FIGURE 4.24

ΔH

Exploiting a GCC pocket for utility substitution.

T*

TCW

−5°C −40°C −70°C ΔH

FIGURE 4.25

Placing refrigeration levels for pure refrigerants.

the GCC. In this case, the Balanced Composite Curves (BCCs) are used. Figure 4.26 shows how the data about the placed utilities can be transferred from the GCC to the BCCs, enabling the correct location of the Utility Pinch associated with LP steam. The BCCs create a combined view in which all heat sources and sinks (including utilities) are in balance and all Pinches are shown.

Process Integration for Improving Energy Efficiency (a) T*

(b) T HP steam

LP steam

HP steam

LP steam

LP steam Pinch

Process Pinch

Process Pinch

LP steam Pinch

CW

CW ΔH Grand Composite Curve

FIGURE 4.26

ΔH Balanced Composite Curve

Locating the LP-steam Utility Pinch.

BCCs are a useful additional tool for evaluating heat recovery, obtaining targets for specific utilities, and planning HEN design regions.

4.4 Extended Pinch Technology 4.4.1 Heat Transfer Area, Capital Cost, and Total Cost Targeting In addition to maximizing heat recovery, it is also possible to estimate the required capital cost. The expressions for obtaining these estimates are derived from the relationship between heat transfer area and the efficiency of a heat exchanger. Methods for targeting capital cost and total cost were initially developed by Townsend and Linnhoff (1984) and further elaborated by others (e.g., Ahmad, Linnhoff, and Smith 1990; Colberg and Morari, 1990; Linnhoff and Ahmad, 1990; Zhu et al., 1995). The HEN capital cost depends on the heat transfer area, the number of the heat exchangers, the number of shell-and-tube passes in each heat exchanger, construction materials, equipment type, and operating pressures. The heat transfer area is the most significant factor, and assuming one-pass shell and tube exchangers it is possible to estimate the overall minimum required heat transfer area; this value helps establish the lower bound on the network’s capital cost. Estimating the minimum heat transfer area is based on the concept of an enthalpy interval. As shown in Figure 4.27, an enthalpy interval is a slice constrained by two vertical lines with fixed values on the ΔH axis. This interval is characterized by its ΔH

69

70

Chapter Four FIGURE 4.27

Enthalpy intervals.

T

Enthalpy interval Amin

=

qstream 1 · ΔTLM streams hstream H

difference, the corresponding temperatures of the CCs at the interval boundaries, its process stream population, and the film heat transfer coefficients of those streams. The minimum heat transfer area target can be obtained by estimating it within each enthalpy interval of the BCCs and then summing up the values over all intervals (Linnhoff and Ahmad, 1990): EI NS ª 1 qs , i º AHEN, min « » « ⌬TLM, i s 1 hs , i ¼» i 1 ¬

¦

¦

Here EI and NS denote the number of enthalpy intervals and the number of streams; i denotes ith enthalpy interval; s, the sth stream; ΔTLM,i, the log-mean temperature difference in interval i (from the CC segments); qs, the enthalpy change of the sth stream; and hs, the heat transfer coefficient of sth stream. The area targets can be supplemented by targets for number of shells (Ahmad and Smith, 1989) and for the number of heat exchanger units, thus providing a basis for estimating the HEN capital cost and the total cost. This approach is known as supertargeting (Ahmad, Linnhoff, and Smith, 1989). With supertargeting it is also possible to optimize the value of ΔTmin prior to designing the HEN. Proposed improvements to the capital cost targeting procedure of Townsend and Linnhoff (1984) mainly involve: (1) obtaining more accurate surface area targets for HENs with nonuniform heat transfer coefficients (Colberg and Morari, 1990; Jegede and Polley, 1992; Zhu et al., 1995; SernaGonzález, Jiménez-Gutiérrez, and Ponce-Ortega, 2007); (2) accounting for construction materials, pressure rating, and different heat exchanger types (Hall, Ahmad, and Smith, 1990); or (3) accounting for safety factors, including “prohibitive distance” (Santos and Zemp, 2000). Further information can be found in the paper by Taal and colleagues (2003), which summarizes the common methods used to estimate the cost of heat exchange equipment and also provides sources of projections for energy prices.

Process Integration for Improving Energy Efficiency

4.4.2 Heat Integration of Energy-Intensive Processes Heat Engines Particularly important processes are the heat engines—steam and gas turbines. They operate by drawing heat from a higher-temperature source, converting part of it to mechanical power; then (after some energy loss) they reject the remaining heat at a lower temperature (see Figure 4.28). For targeting purposes the energy losses are usually neglected. Integrating a heat engine across the Pinch, which is equivalent to a Cross-Pinch process-to-process heat transfer, results in a simultaneous increase of hot and cold utility, which usually leads to excessive capital investment for the utility exchangers. If a heat engine is integrated across the Pinch, then the hot utility requirement is increased by Q and the cold by Q − W (in the notation of Figure 4.28). Heat engines should be integrated in one of two ways. 1. Above the Pinch (Figure 4.29a): This increases the hot utility for the main process by W, but this extra heat is converted into shaftwork. 2. Below the Pinch (Figure 4.29b): This offers a double benefit. It saves on a cold utility, and the process heat below the Pinch supplies Q to the heat engine (instead of rejecting it to a cooling utility). Different heat engines differ in their placement. On the one hand, steam turbines may be placed either below or above the Pinch because they draw and exhaust steam. Figure 4.30 shows steam turbine integration above the Pinch, which has the benefit of cogenerating

T*

T*source

Source Q

W

Q–W T*sink Sink

FIGURE 4.28

Heat engine configuration.

71

72

Chapter Four A+W

T*

T* A–(Q –W)

A

Q HE

Q –W

PINCH

W

PINCH

HE

B–Q

Integration above the pinch (a)

FIGURE 4.29

W

Q–W

100% conversion Heat→Work

B

100% conversion Heat→Work Q

Integration below the pinch (b)

Appropriate placement of heat engines.

HP Steam

T*

W

QHP QLP

QHP

T* QFUEL

LP Steam

Boiler

QLP

Condensate PINCH

CW ΔH

QC,min

FIGURE 4.30

Integrating a steam turbine above the Pinch.

extra power. In contrast, gas turbines—which use fuel as input—are typically used only as a utility heat source for the processes and can be placed only above the Pinch.

Heat Pumps Heat pumps present another opportunity for improving the energy performance of an industrial process. Their operation is the reverse of heat engines. That is, heat pumps take heat from a lowertemperature source, upgrade it by applying mechanical power, and then deliver the combined flow to a higher-temperature heat sink (Figure 4.31). An important characteristic of heat pumps is their coefficient of performance (COP). This metric for device efficiency is defined as the

Process Integration for Improving Energy Efficiency FIGURE 4.31 Heat-pump configuration.

T*

Sink Q + W = 125 kW

T*sink

W = 25 kW Q = 100 kW T*source

Source

ratio between the heat delivered to the heat sink and the consumed shaftwork (mechanical power): Q sink

Q source  W

(4.6)

COP

Q sink Q source  W = W W

(4.7)

The COP is a nonlinear function of the temperature difference between the heat sink and the heat source (Laue, 2006); this difference is also referred to as temperature lift. Figure 4.32(a) shows the appropriate integration of a heat pump across the Pinch, with the heat source located below the Pinch and the heat sink above it. The GCC facilitates sizing of the heat pump by evaluating the possible temperatures of the heat source and heat sink, and their loads; see Figure 4.32(b). Integrating entirely above the Pinch results in direct conversion of mechanical power to heat. This is a waste of resources because most of the power is generated at the expense of two to three times the amount of fuel energy. The second alternative—placing the heat pump entirely below the Pinch—results in the power flow consumed by the heat pump being added to the cooling utility demand below the Pinch. The procedure for sizing heat pumps to be placed across a (process or utility) Pinch is illustrated in Figure 4.33. First, temperatures are chosen for the heat source and the heat sink. Then the horizontal projections spanning from the temperature axis to the GCC provide the maximum values for the heat source and sink loads. Recall that the GCC shows shifted temperatures. Because real temperatures are used when calculating the heat-pump temperature lift, the GCC values must be modified by subtracting or adding ΔTmin/2 (see Section 4.3.3). The COP value can be derived from the calculated ΔTpump and can be then used to calculate the necessary duties.

73

74

Chapter Four QHmin – (QHP + W)

(a) T*

Steam

(b) T*

QHP + W

QHP +W

PINCH QHP

HEAT PUMP

W

W QHP CW

Qcmin – QHP Appropriate placement

FIGURE 4.32

ΔH Load and temperature lift on the GCC

Heat pump placement against a heat recovery problem.

T*

QHP + W

5

COP

W 6

MAX

QHP + W W QHP

2 3 T*SINK ½ΔTmin ΔTPUMP

T*SOURCE 1 MAX

4

4

3 ΔH

FIGURE 4.33

ΔTPUMP

Procedure for heat-pump sizing.

As a specific example, assume that the GCC in Figure 4.34 reflects an industrial process with ΔTmin = 20°C and that a heat pump is available, described as follows: 0.874 COP 100.18 ˜ ⌬Tpump

(4.8)

Focusing on the Pinch “nose” (a sharp nose provides a better integration option) allows choosing a shifted temperature for the heat source, in this example: T*source = 85˚C; see Figure 4.35. Using this value allows extracting a maximum of 6.9 MW from the GCC below the Pinch. Setting T *sink = 100˚C results in an upper bound of 2.634 MW for the sink load. Transforming to real temperatures and taking the difference yields a temperature lift of ΔTpump = 35°C. By Eq. (4.8), the COP is thus equal to 4.4799. Given the upper bounds on the sink

Process Integration for Improving Energy Efficiency ΔH[MW]

T*[°C]

21.90

440

29.40

410

23.82

131

18.00

118

ΔTMIN = 20°C 500 450 400 350 300 T*[°C] 250

1.80

115

0.00

94

150

4.30

91

100

11.50

79

15.00

30

200

50 0 0

10

20

30

40

20

25

ΔH [MW]

FIGURE 4.34

Heat-pump sizing example: Initial data of the GCC.

FIGURE 4.35 Heat-pump sizing example: Attempt 1.

140 120 QSINK T* [°C]

100

Maximum

80 QSOURCE

60 40 20 0

5

10

15

ΔH [MW]

and source heat loads, the smaller one is chosen as a basis. Here the sink bound is smaller, so the sink is sized to its upper bound: Qsink = Qsink,max = 2.634 MW. From this, the required pump power consumption is computed to be 0.588 MW. As a result, the actual source load for the heat pump is 2.046 MW. Comparing this value with the upper bound of 6.9 MW, it is evident that the source heat availability is considerably underutilized. A different selection of source and sink temperatures is needed if the source availability is to be better utilized. As a second attempt, the sink temperature is increased from 100°C to 110°C. The maximum source heat remains 6.9 MW, but the maximum sink capacity increases from 2.634 to 7.024 MW. This results in the desired

75

Chapter Four temperature lift of ΔTpump = 45°C; the COP is now 3.5964, W = 2.657 MW, and the sink load Qsink = 9.557 MW; see Figure 4.36. However, the heat sink is oversized in this case (Figure 4.36), so the heat source temperature has to be shifted upward. An increase of 2.28°C (see Figure 4.37) yields the following values: T *source = 87.28˚C; ΔTpump = 42.72°C; a maximum source load (also taken as the selected source load) of 5.152 MW; a maximum sink load equal to the selected sink load of Qsink = 7.016 MW; COP = 3.7637; and W = 1.864 MW. Better results can be obtained by optimizing the two temperatures simultaneously while using the overall utility cost as a criterion. 140 QSINK

120

T* [°C]

100 The sink is oversized 80 QSOURCE

60 40 20 0

5

10

15

20

25

20

25

ΔH [MW]

FIGURE 4.36

Heat-pump sizing example: Attempt 2.

140 QSINK

120 100 T* [°C]

76

80 QSOURCE 60 40 20 0

5

10

15

ΔH [MW]

FIGURE 4.37

Heat-pump sizing example: Attempt 3.

Process Integration for Improving Energy Efficiency Once utility levels are chosen, the heat pump can be placed also across a Utility Pinch (Figure 4.38). A special case of integration involves the placement of refrigeration levels (Figure 4.39). Refrigeration facilities are heat pumps whose main value is that their cold end absorbs heat. Utilizing their hot ends for process heating can save considerable amounts of hot utility, especially when relatively low-temperature heating is needed.

Distillation Processes and Other Separations The simplest distillation column includes one reboiler and one condenser, and these components account for most of the column’s T*

HP

MP

IP LP

CW ΔH

FIGURE 4.38

Heat-pump placement across the utility Pinch. T*

Rcond W

HEAT PUMP

CW

0 R1 R2 ΔH

FIGURE 4.39

Refrigeration systems.

77

78

Chapter Four energy demands. For purposes of Heat Integration, the column is represented generally by a rectangle: the top side denotes the reboiler as a cold stream, and the bottom side denotes the condenser as a hot stream; see Figure 4.40. There are three options for integrating distillation columns: across the Pinch, as shown in Figure 4.41(a); and entirely below or entirely above the Pinch, as shown in Figure 4.41(b). Integrating across the Pinch only increases overall energy needs, so this option is not useful. The other two options result in net benefits by eliminating the need to use an external utility for supplying the distillation reboiler (above the Pinch) or the condenser (below the Pinch). The GCC is used to identify the appropriate column integration options. Figure 4.42 illustrates two examples of appropriately placed distillation columns.

T* A

Reboiler

A, B

Condenser

B

H

FIGURE 4.40 Distillation column: T–H representation.

(a) T*

A + QDIST

A

(b) T*

QDIST

QDIST

PINCH

PINCH Q

DIST

QDIST B + QDIST Across the pinch

FIGURE 4.41

QDIST

QDIST B Below or above the pinch

Distillation column: Integration options.

Process Integration for Improving Energy Efficiency FIGURE 4.42 Appropriate placement of distillation columns against the GCC.

T*

ΔH

When the operating conditions of a column result in placing it across the Pinch, there are several degrees of freedom that can be utilized to facilitate appropriate placement. It may be possible to change the operating pressure, which could shift the column with respect to the temperature scale until it fits above or below the Pinch. Varying the reflux ratio results in simultaneous changes of the column temperature span and the duties of the reboiler and condenser. Increasing the reflux ratio (the ratio between the reflux flowrate returned to the column and the distillate product flowrate) yields a smaller temperature span and larger duties, whereas reducing the ratio has the opposite effect. It is also possible to split the column into two parts, introducing a “double effect” distillation arrangement. In this approach, one of the effects is placed below and the other above the Pinch; this prevents internal thermal integration of the column effects. Additional options are available, such as interreboiling and intercondensing. When using available degrees of freedom, it is important to keep in mind that the energy–capital trade-offs of the column and the main process are combined and thus become more complicated than the individual trade-offs. Another important issue is controllability of the integrated designs: unnecessary complications should be avoided, and disturbance propagation paths should be discontinued. It is usually enough to integrate the reboiler or the condenser. If inappropriate column placement cannot be avoided, then condenser vapor recompression with a heat pump can be used to heat up the reboiler. Evaporators constitute another class of thermal separators. Because they, too, feature a reboiler and a condenser, their operation is similar to that of distillation columns and so the same integration principles can be applied to them. Absorber-stripper loops and

79

80

Chapter Four dryers are similarly integrated. This subject has been extensively studied by Kemp (2007, sections 6.3 to 6.5).

4.4.3

Process Modifications

The basic Pinch Analysis calculations assume that the core process layers in the onion diagram (Figure 4.2) remain fixed. However, it is possible—and in some cases beneficial—to alter certain properties of the process. Properties that can be exploited as degrees of freedom include: (1) the pressure, temperature, or conversion rate in reactors; (2) the pressure, reflux ratio, or pump-around flow rate in distillation columns; and (3) the pressure of feed streams in evaporators. Such modifications will also alter the heat capacity flow rates and temperatures of the related process streams for Heat Integration; this will cause further changes in the shapes of the CCs and the GCC, thereby modifying the utility targets. The CCs are a valuable tool for suggesting beneficial process modifications (Linnhoff et al., 1982). Figure 4.43 illustrates this application of the CCs in terms of the plusminus principle. The main idea is to alter the CC’s slope in the proper direction in order to reduce the amount of utilities needed. This can be achieved by changing CP (e.g., by mass flow variation). According to Smith (2005), such decreases in utility requirements can be brought about by (1) increases in the total hot stream duty above the Pinch, (2) decreases in the total cold stream duty above the Pinch, (3) decreases in the total hot stream duty below the Pinch, and/or (4) increases in the total cold stream duty below the Pinch. Another guide to modifying processes is the principle of keep hot streams hot (KHSH) and keep cold streams cold (KCSC). As illustrated in Figure 4.44, increasing the temperature differences by process

T

+ − − +

ΔH

FIGURE 4.43

The plus–minus principle.

Process Integration for Improving Energy Efficiency T

T

ΔH

ΔH Hot streams (a)

FIGURE 4.44

Cold streams (b)

(a) Keep hot streams hot; (b) keep cold streams cold.

modification allows for more overlap of the curves and results in improved heat recovery. In particular, energy targets improve if the heating and cooling demands can be shifted across the Pinch. The principle suggests (1) shifting hot streams (cooling demands) from below to above the Pinch and/or (2) shifting cold streams (heating demands) from above to below the Pinch. See Chapter 12 (and Figure 12.7) for more details.

4.5 HEN Synthesis Most industrial-scale methods synthesize heat recovery networks under the assumption of a steady state.

4.5.1 The Pinch Design Method The Pinch Design Method (Linnhoff and Hindmarsh, 1983) became popular owing to its simplicity and efficient management of complexity. The method has evolved into a complete suite of tools for heat recovery and design techniques for energy efficiency, including guidelines for changing and integrating a number of energy-intensive processes.

HEN Representation The representation of HENs by a general process flowsheet, as in Figure 4.45, is not always convenient. The reason is that this representation makes it difficult to answer a number of important questions: “Where is the Pinch?” “What is the degree of heat recovery?” “How much cooling and heating from utilities is needed?” The so-called conventional HEN flowsheet (Figure 4.46) offers a small improvement. It shows only heat transfer operations and is based on a simple convention: cold streams run horizontally and hot

81

82

Chapter Four Feed 2

4

140°C

3 230°C Reactor 2 250°C Product 2

180°C Reactor 1

80°C Off-Gas

Feed 1

40°C

1

20°C 40°C

2

Product 1, 40°C

FIGURE 4.45 Using a general process flowsheet to represent a HEN.

FIGURE 4.46 Conventional HEN flowsheet.

2

250°C

4

12.5 MW

140°C

3

200°C

181.7°C 230°C

205°C

H

7.0 MW

7.5 MW

203.3°C

150°C 8.0 MW

150°C

6.5 MW 1

140°C 52.5°C

106.7°C

20°C C

10.0 MW 40°C

180°C

17.5 MW Above the Pinch 80°C

streams vertically. Although the Pinch location can be marked for simple cases, it is still difficult to see. This representation makes it difficult to express the proper sequencing of heat exchangers and to represent clearly the network temperatures. Furthermore, changing

Process Integration for Improving Energy Efficiency the positions of some matches often results in complicated path representations. The grid diagram, as shown in Figure 4.47, provides a convenient and efficient representation of HENs by eliminating the problems just described. The grid diagram has several advantages: the representation of streams and heat exchangers is clearer, it is more convenient for representating temperatures, and the Pinch location (and its implications) are clearly visible; see Figure 4.48. As in the conventional HEN flowsheet, only heat transfer operations are shown in the grid diagram. Temperature increases from left to right in the grid, which is intuitive and in line with CC diagrams, making (re)sequencing heat exchangers are straightforward.

The Design Procedure The procedure for designing a HEN follows several simple steps: 1. Specification of the heat recovery problem. (a)

HOT 1 HOT 2 COLD 1 COLD 2

H Simplified view

(b)

MP Steam HOT 1 HOT 2

C

COLD 1 COLD 2

H

CW Showing the utility streams explicitly

FIGURE 4.47

H

Hot utility

C

Cold utility

The grid diagram for HENs.

Heat exchange between streams

83

84

Chapter Four 2. Identification of the heat recovery targets and the heat recovery Pinch, as explained in Section 4.3. 3. Synthesis 4. Evolution of the HEN topology The first two steps were discussed in previous sections. The synthesis step begins by dividing the problem at the Pinch and then positioning the process streams as shown in Figure 4.49. The engineering practice suggests starting the network design from the Pinch (the most restricted part of the design owing to temperature differences approaching ΔTmin) and then to place heat exchanger matches while moving away from the Pinch (Figure 4.50). When placing matches, several rules have to be followed in order to obtain a network that minimizes utility use: (1) no exchanger may have a temperature difference smaller than ΔTmin;

No cross-Pinch heat transfer

A cross-Pinch heat transfer match

C C

H H

FIGURE 4.48

The grid diagram and implications of the Pinch.

CP [kW/°C]

PINCH 150°C

40°C 80°C

1

20°C

150°C

140°C 3

140°C

QHmin = 750 kW

FIGURE 4.49

250°C 200°C

2

4

180°C

15 25

20 230°C

30

QCmin = 1000 kW

Dividing at the Pinch for the streams in Table 4.2.

Process Integration for Improving Energy Efficiency T

PINCH

ΔH

FIGURE 4.50

Pinch design principle.

(2) no process-to-process heat transfer may occur across the Pinch; and (3) no inappropriate use of utilities should occur. At the Pinch, the enthalpy balance restrictions entail that certain matches must be made if the design is to achieve minimum utility usage without violating the ΔTmin constraint; these are referred to as essential matches. Above the Pinch, the hot streams should be cooled only by transferring heat to cold process streams, not to utility cooling. Therefore, all hot streams above the Pinch have to be matched up with cold streams. This means that all hot streams entering the Pinch must be given priority when matches are made above the Pinch. Conversely, cold streams entering the Pinch are given priority when matches are made below the Pinch. Now recall the example from Table 4.2. Figure 4.49 shows the scaled grid diagram, indicating the hot and cold Pinch temperatures. The part above the Pinch requires essential matches for streams 2 and 4, since they are entering the Pinch. Consider stream 4. One possibility is to match it against stream 1, as shown in Figure 4.51. Stream 4 is the hot stream, and its CP is greater than the CP for cold stream 1. As shown in the figure, at the Pinch the temperature distance between the two streams is exactly equal to ΔTmin. Moving away from the Pinch results in temperature convergence because the slope of the hot stream line is less steep owing to its larger CP. Since ΔTmin is the lower bound on network temperature differences, the proposed heat exchanger match is infeasible and thus is rejected. Another possibility for handling the cooling demand of stream 4 is to implement a match with stream 3, as shown in Figure 4.52. The CP of stream 3 is larger than the CP of stream 4, resulting in divergent

85

86

Chapter Four CP [kW/°C]

PINCH 150°C 150°C

250°C 200°C

2

3

140°C 140°C

CPHOT > CPCOLD

15 PINCH

4

4

25

HEAT EXCHANGER MATCH 1

T

ΔTmin 1

180°C

20 230°C

ΔH Temperature difference smaller than ΔTmin

30

INFEASIBLE!

FIGURE 4.51

An infeasible heat exchanger match above the Pinch.

PINCH

CP [kW/ºC] 250ºC

150ºC

150ºC

200ºC

T 2

15

PINCH 4

4

25

HEAT EXCHANGER MATCH 1

140ºC 140ºC

3

FIGURE 4.52

3 ΔTmin

180ºC

20 230ºC

ΔH The match is feasible

30

A feasible heat exchanger match above the Pinch.

temperature profiles in the direction away from the Pinch. Thus, the rule above the Pinch may be expressed as follows: CPhot stream d CPcold stream

(4.9)

The logic below the Pinch is symmetric. This part of the design is a net heat source, which means that the heating requirements of the cold streams have to be satisfied by matching up with hot streams. The same type of reasoning as before yields the following requirement: the CP value of a cold stream must not be greater than the CP value

Process Integration for Improving Energy Efficiency of a hot stream if a feasible essential match is to result. Generalizing Eq. (4.9) shows that the CP of the stream entering the Pinch must be less than or equal to the CP of the stream leaving the Pinch: CPentering pinch d CPleaving pinch

(4.10)

The Pinch Design Method incorporates a special tool for handling this stage: CP tables (Linnhoff and Hindmarsh, 1983). Here the streams are represented by their CP values, which are sorted in descending order. This facilitates the identification of promising combinations of streams for candidate essential matches. Sizing the matches follows the so-called tick-off heuristic, which stipulates that the heat exchange match should be as large as possible so that at least one of the involved streams will be completely satisfied and then “ticked off” from the design list; see Figure 4.53.

Completing the Design The HEN design above the Pinch is illustrated in Figure 4.54. The design below the Pinch follows the same basic rules, with the small difference that here it is the cold streams that define the essential matches. Figure 4.55 details the design below the Pinch for the considered example. First the match between streams 4 and 1 is placed and sized to the duty required by stream 4. The other match, between streams 2 and 1, formally violates the Pinch rule for placing essential matches. However, since stream 1 already has another match at the Pinch, the current match (between 4 and 1) is not strictly termed essential. Up

CP [kW/ºC] 150ºC

203.3ºC

250ºC

150ºC

200ºC

140ºC

180ºC

1

QSTREAM [kW]

2

15

1500

4

25

1250

20

800

30

2700

800 kW 140ºC 3

1250 kW

FIGURE 4.53

230ºC

TX = 181.7ºC TX =140 +

The tick-off heuristic.

1250 30

=181.7ºC

87

88

Chapter Four

150°C

203.3°C

150°C

250°C

200°C

2

4

CP [kW/°C]

QSTREAM [kW]

15

1500

25

1250

20

800

30

2700

180°C

140°C 1 800 kW 140°C

TX = 181.7°C

3

1250 kW

FIGURE 4.54

205°C 700 kW

H

230°C

750 kW

The HEN design above the Pinch. CP QSTREAM [kW/°C] [kW]

40°C

C

150°C

106.7°C

2

15

1650

4

25

1750

20

2400

1000 kW 150°C

80°C

1

52.5°C

20°C 650 kW

FIGURE 4.55

140°C 1750 kW

The HEN design below the Pinch.

to the required duty of 650 kW, this match does not violate the ΔTmin constraint, which is the relevant one. The completed HEN topology is shown in Figure 4.56. It is not always possible to follow the basic design rules described previously, so in some cases it is necessary to split the streams so that heat exchange matches can be appropriately placed. Splitting may be required in the following situations: 1. Above the Pinch when the number of hot streams is greater than the number of cold streams (NH > NC); see Figure 4.57. 2. Below the Pinch when the number of cold streams is greater than the number of hot streams (NC > NH); see Figure 4.58. 3. When the CP values do not suggest any feasible essential match; see Figure 4.59.

Process Integration for Improving Energy Efficiency CP [kW/°C]

PINCH 150°C

106.7°C C 1000 kW 80°C

40°C

1

203.3°C

150°C

20°C

200°C

4

140°C

Tx =181.7 °C

205°C

QCmin =1000 kW

QHmin = 750 kW

Completed HEN design.

(a)

CP [kW/°C]

PINCH 100°C 1

12

2

20

3

7

100°C 100°C I?

5

90°C

T > 90°

90°C

T > 90°

15 30 More Hot Streams than Cold Streams

(b) CP [kW/°C]

PINCH 100°C 1

12

2

20

3

7

100°C 100°C 90°C 4

15 90°C

5

30

Split a cold stream

FIGURE 4.57

25 20

230°C 30 H 700 kW 750 kW

1250 kW

4

15

800 kW

650 kW 1750 kW 3

2

180°C

140°C

52.5°C

FIGURE 4.56

250°C

Splitting above the Pinch for NH > NC .

89

90

Chapter Four CP [kW/°C]

PINCH T3

b2={0,0.5,0} control systems

time>5

b0

r3={1,0,0}

r2={1,0,0}

r1={0,1,0}

R=50

212

emf

3rd Order

Line2

G2

Composition diagrams produced using Modelica (2009b).

Sof tware Tools this lead time is a primary objective of the European Commission’s Directorate-General for Transport and Energy (DGTREN), which has funded two related projects, EMINENT (Early Market Introduction of New Energy Technologies) and EMINENT2 (Klemeš et al., 2005b). The principal features of these projects are a software tool and an integrated database of new technologies and sectoral energy supplies and demands. The software tool is for analyzing the potential impact of new and underdeveloped energy technologies emerging in different sectors from different countries. This tool has also been used in case studies that illustrate the new technologies. The aim of the EMINENT software is to assess the market potential of early-stage technologies (ESTs) in various energy supply chains by evaluating their performance in terms of: (1) CO2 emissions, (2) costs of energy supply, (3) use of primary fossil energy, and (4) effects on different subsectors of society. Technology developers and financial supporters are frequently not aware of all the potential applications or the relative market attractiveness of such technology across different countries and sectors of society. Thus, the EMINENT project provides insight into the market potential that can accelerate the development of technologies; this benefits research and development efforts by targeting them more effectively. The EMINENT tool that evaluates ESTs makes use of two databases: (1) national energy infrastructures, which contain information on the number of consumers per sector, type of demand, typical quality of the energy required, and consumption and installed capacity per end user and (2) other ESTs and technologies that are already commercial— including key information on new energy technologies currently under development and proven energy technologies now available and in use. The availability, price, and geographical conditions of primary energy resources differ significantly worldwide, so the impact of ESTs can be evaluated only within the context of a particular (national) energy supply system (Klemeš et al., 2007b). The EMINENT package consists of an integrated resource manager, a demand manager, and an EST manager as well as databases on resources and demand. The methodology, as shown in Figure 9.11, can be briefly summarized as follows: Resource manager selects, enters, and modifies data on country resources (electrical, fuel-based, geothermal, hydro, ocean tidal, wave, and wind energy). Demand manager describes energy demands per subsector in a given country; it selects data for the technology assessment, enters new data, and modifies old data. Technology manager stores key data on existing technologies and ESTs. User input: (1) The sectoral energy demands whose potential supply by EST is being evaluated; (2) any other peripheral technologies

213

214

Chapter Nine Solar

Hydro

Coal

Gas/Oil Hydrogen

Wind

Ground Heat

Biomass

Apply EMINENT tool to assess the new technology potential Energy supply system Intermediate products Biomass/waste Coal Oil

Pretreatmentsystems

Electricity Transportation and storage

Conversion processes

Natural gas Hydro Wind

EST to be evaluated

Distribution and storage

Heat

Transportation fuel

Solar energy Geothermal

FIGURE 9.11 2007b).

Methodology employed in EMINENT toolbox (after Klemeš et al.,

needed to establish full energy supply chains; and (3) resources the EST would require to satisfy the full energy supply chain. Output: (1) aggregate numbers; (2) application potential of ESTs per (sub)sector; (3) annual cost of energy delivery per consumer and per (sub)sector; and (4) annual CO2 emissions. Performance indicators: (1) efficiency of energy supply chain; (2) usage of primary fossil energy; (3) CO2 emissions per MW∙h; and (4) costs of delivered energy [€/MW∙h]. Most of the ESTs analyzed were not yet able to achieve the cost levels of existing technologies. Some of the ESTs—for instance, molten carbonate fuel cells (MCFCs)—could become competitive with relatively small efforts aimed at cost reduction. Various promising future trends located with the help of EMINENT have been supported by policy makers. Some near-term prospects are: (1) diverse energy systems that encompass supplies, management, and control of demand; (2) market-based grids with large power stations, including wind farms of different types; (3) local distributed generation, including biomass, waste, and wind; (4) micro generation,

Sof tware Tools including Combined Heat and Power (CHP), fuel cells, and photovoltaic technology; new homes built with nearly zero carbon emissions; (6) natural gas; (7) coal-fired generation combined with carbon capture and storage; and (8) mixed fuels (e.g., coal mixed with biomass, natural gas mixed with hydrogen). Longer-term prospects include nuclear power stations, fuel cells, hydrogen obtained from nonelectricity sources (e.g., biomass, low-carbon biofuels), and nuclear fusion.

9.8.3 Balancing and Flowsheeting Simulation for Energy-Saving Analysis Tools for balancing, reconciliation, and flowsheeting simulation are frequently used for energy-saving analysis and have become an essential item in the process engineer’s toolbox. These tools help designers develop complete mass and energy models based on actual measurements and/or design values and mathematical models. As a result, these simulation tools play an important role in the technical and economic decision making related to the planning and design stages of processes under development and to the operation of existing equipment. Several computer-based systems have been developed over the years in order to assist process engineers with energy and mass balance calculations. However, ongoing development costs have resulted in a limited number remaining on the market, and these have been secured only by a substantial volume of sales. An early overview of the field was presented by Klemeš (1977). The technology used for balancing and for data validation and reconciliation consists of a set of procedures incorporated into a software tool. Process data reconciliation has become the main method for monitoring and optimizing industrial processes as well as for performing component diagnosis, condition-based maintenance, and online calibration of instrumentation. According to Heyen and Kalitventzeff (2007), reconciliation has three main goals: (1) detect and correct deviations and errors of measurement data so that all balance constraints are satisfied; (2) exploit the structure of and knowledge about the process system by using measured data to estimate unmeasured data whenever possible, in particular as regards key performance indicators (KPIs); and (3) determine the postprocessing accuracy of measured and unmeasured data, including KPIs. A comprehensive system called DEBIL—which included balancing, flowsheeting simulation, and optimization—was created several decades ago (see Klemeš, Luťcha, and Vašek, 1979) and has since been further developed by Belsim into the balancing and reconciliation tool VALI (VALI III User Guide, 2003). This tool has been applied to various energy-efficiency tasks, as reported with respect to nuclear power plants (Langenstein, Jansky, and Laipple, 2004) and regenerative heat exchangers (Minet et al., 2001).

215

216

Chapter Nine

9.8.4 Integrating Renewable Energy into Other Energy Systems There are many different computer tools now available that can be used to analyze the integration of renewable energy. Connolly and colleagues (2010) have reviewed these tools in considerable detail. Their study analyzed 37 computer tools designed for this purpose, as summarized (in alphabetical order) in Table 9.1.

Tool (availability)

Applications

Reference

AEOLIUS (commercial)

Power plant dispatch simulation tool

Universität Karlsruhe (2009)

BALMOREL (free download)

Open-source electricity and district heating tool

Balmorel (2009)

BCHP Screening Tool (free download)

Assesses CHP in buildings

Oak Ridge National Laboratory (2009a)

COMPOSE (free download)

Single-project technoeconomic assessments

Aalborg University (2009a)

E4cast (commercial)

Tool for energy projection, production, and trade

ABARE (2009)

EMCAS (commercial)

Creates techno-economic models of the electricity sector

Argonne National Laboratory (2009a)

EMINENT (registration required)

Early-stage technologies assessment

EMINENT2 (2009)

EMPS (commercial)

Electricity systems with thermal/hydro generators

SINTEF (2009b)

EnergyPLAN (free download)

User-friendly analysis of national energy systems

Aalborg University (2009b)

energyPRO (commercial)

Single-project technoeconomic assessments

EMD International A/S (2009)

ENPEP-BALANCE (free download)

Market-based energysystem tool

Argonne National Laboratory (2009b)

GTMax (commercial)

Simulates electricity generation and flows

Argonne National Laboratory (2009c)

H2RES (internal use only)

Energy-balancing models for island energy systems

Instituto Superior Técnico (2009)

HOMER (free download)

Techno-economic optimization for standalone systems

HOMER (2009)

TABLE 9.1

Software Tools for Analyzing the Integration of Renewable Energy into Other Energy Systems (after Connolly et al., 2010)

Sof tware Tools Tool (availability)

Applications

Reference

HYDROGEMS (free for TRNSYS users)

Renewable and H2 standalone systems

Institute for Energy Technology (2009)

IKARUS (earlier versions are free)

Bottom-up cost optimization tool for national systems

Forschungszentrum Jülich Institute for Energy Research (2009)

INFORSE (free to nongovernmental organizations)

Energy-balancing models for national energy systems

INFORSE-Europe (2009)

Invert (free download)

Simulates promotion schemes for renewable energy

Vienna University of Technology (2009)

LEAP (free for developing countries and for students)

User-friendly analysis for national energy systems

Stockholm Environment Institute (2009)

MARKAL/TIMES (commercial)

Energy–economic tools for national energy systems

International Energy Agency (2009)

MESAP PlaNet (commercial)

Linear network models of national energy systems

Schlenzig (2009)

MESSAGE (free except for the simulators)

Medium- and long-term assessment of national or global energy systems

International Institute for Applied Systems Analysis (2009)

MiniCAM (free download)

Simulates long-term, large-scale global changes

MiniCAM (2009)

NEMS (free except for the simulators)

Simulates the U.S. energy market

Energy Information Administration (2009)

ORCED (free download)

Simulates regional electricity dispatch

Oak Ridge National Laboratory (2009b)

PERSEUS (sold to large European utilities)

Family of energy and material flow tools

Universität Karlsruhe (2009)

PRIMES (projects are undertaken for a fee)

Market equilibrium tool for energy supply and demand

National Technical University of Athens (2009)

ProdRisk (commercial)

Optimizes operation of hydro power

SINTEF (2009a)

RAMSES (projects are undertaken for a fee)

Simulates the electricity and district heating sector

Danish Energy Agency (2009)

RETScreen (free download)

Renewable analysis for electricity and/or heat in systems of any size

National Resources Canada (2009)

TABLE 9.1

Software Tools for Analyzing the Integration of Renewable Energy into Other Energy Systems (Continued)

217

218

Chapter Nine

Tool (availability)

Applications

Reference

SimREN (projects are undertaken for a fee)

Bottom-up supply and demand for national energy systems

Institute for Sustainable Solutions and Innovations (2009)

SIVAEL (free download)

Electricity and district heating sector tool

Energinet.dk (2009)

STREAM (free download)

Overview of national energy systems to create scenarios

Ea Energy Analyses (2009)

TRNSYS16 (commercial)

Modular structured models for community energy systems

TRNSYS (2009)

UniSyD3.0 (contact [email protected])

National energy systems scenario tool

Unitec New Zealand (2009)

WASP (free to IAEA member states)

Identifies the least-cost expansion of power plants

IAEA (2009)

WILMAR Planning Tool (commercial)

Increasing the use of wind in national energy systems

Risø National Laboratory (2009)

TABLE 9.1

Software Tools for Analyzing the Integration of Renewable Energy into Other Energy Systems (Continued)

CHAPTER

10

Examples and Case Studies

T

his chapter provides a selection of problems that have been collected by the authors over twenty years of teaching and consulting. The problems include step-by-step solutions, which provide guidance for mastering the methodology. Space limitations make it impossible to cover all aspects or to provide fully comprehensive solutions, for which an entire book would be required. The representative problems selected for presentation here are divided into five groups: Heat Pinch Technology, Total Sites, integrated placement of processing units, utility placement, and Water Pinch Technology.

10.1 Heat Pinch Technology The first group of problems involves heat Process Integration, known also as Heat (and, in Australia and South Africa, as Thermal) Pinch Technology.

10.1.1 Heat Pinch Technology: First Problem Problem 1: Task Assignment A chemical process is served by a Heat Exchanger Network (HEN), as displayed in Figure 10.1. The figure shows the supply and the target temperatures at the start and end of each stream. For this problem, the minimum allowed temperature difference ΔTmin = 10°C. The following tasks should be performed: (a) Completion of the network description. (1) Convert the network representation to a grid diagram. (2) Calculate the missing temperatures and heat loads for the recovery heat exchangers, heaters, and coolers. (b) Identification of the Network Pinch. (1) Find and write down a path that connects a heater and a cooler through a recovery heat exchanger. Derive expressions for the heat loads and

219

220

Chapter Ten 140°C

164°C 125°C

170°C

300°C H

H CP [kW/°C] 100 H1

190°C

337°C

C

160°C

160 H2 220°C

50 H3

190 H4

220°C

C

C

100°C

FIGURE 10.1

60°C

45°C

160°C

CP [kW/°C]

40°C

35°C

80°C

60°C

140°C

C1

C2

C3

C4

C5

100

70

175

60

200

Existing Heat Exchanger Network (Problem 1).

temperatures that will vary with shifting amounts of heat X [kW] through the path in order to increase the heat recovery. (2) Shift the maximum amount of load through the path while accounting for the minimum allowed temperature difference. Write down the maximum shifted load, the pinching exchanger, and the stream temperatures for the exchanger. Using the Pinch method yields the Maximum Energy Recovery (MER) targets listed in Table 10.1 and the Grand Composite Curve (GCC) shown in Figure 10.2. (c) Identification of the scope for improvement. (1) Calculate the scope for improvement in heat recovery in terms of the network’s total heating requirement. (2) Find the heat exchangers, implementing cross-Pinch heat transfer, and write them down. Problem 1: Solutions Answer to (a)(1) and (a)(2). The HEN is represented as a grid diagram in Figure 10.3, which also shows the missing HEN parameters (i.e., temperatures and loads). Answer to (b)(1). A path between a cold and a hot utility is called a utility path. Heat duty can be shifted along a utility path, which provides a degree of freedom in the HEN retrofit. Figure 10.4 shows a utility path connecting a heater and a

Examples and Case Studies Interval

T * [°C]

Enthalpy [MW]

1

332

17,780

2

305

20,480

3

215

2,480

4

175

2,880

5

169

2,580

6

155

900

7

145

0 (Pinch)

8

130

1,650

9

105

25

10

85

725

11

65

4,925

12

55

7,625

13

40

10,925

14

35

11,425

TABLE 10.1

Calculated MER Heat Cascade for Problem 1

ΔTmin = 10°C 350 300

T* [°C]

250 200 150 100 50 0 0.0

5.0

10.0 ΔH [MW]

FIGURE 10.2

Grand Composite Curve for Problem 1.

15.0

20.0

221

222

Chapter Ten 99.7°

40.0°

190.0° 337.0° E2 E1

C3 5970 kW

160.0°

220.0°

E4 60.0°

88.0° C6

45.0°

C1 C2 C3 C4 C5

220.0°

E5 118.55° E7 C10

160.0°

H1

100

H2

160

H3

50

H4

190

300.0° H8 14700 kW 5300 kW 164.0° 247.0°

100.0° 35.0°

9030 kW

80.0°

125.0°

7875 kW

60.0°

170.0°

6600 kW

140.0°

300.0°

188.0°

H9

9600 kW

FIGURE 10.3

CP [kW/°C]

100 70 175 60 200

22400 kW

Calculated grid diagram for Problem 1.

Load-shift path CP [kW/°C] 40.0°

C3

E2

TH11

E1

H1

100

220.0°

E4

H2

160

H3

50

88.0° 220.0°

E5

C6

1400 kW 118.55° 45.0° C10

160.0°

E7

13984 kW

100.0° C1

QE1 C2

337.0°

QC3

160.0° 60.0°

TH12

TC11 H8 QH8

80.0°

9030 kW

C3 7875 kW

C4 C5

140.0°

6600 kW

188.0° 9600 kW

FIGURE 10.4

300.0°

TC2,out=164.0°

TC2,in=35.0°°

60.0°

190

H4

H9 22400 kW

The load-shift path identified for Problem 1.

100 70

125.0°

175

170.0°

60

300.0°

200

Examples and Case Studies cooler through a heat recovery exchanger. The temperatures, which will vary with the amount of heat shifted, are also indicated in the figure. The expressions for the variation in the affected heat loads and temperatures in response to a shifted load of X kW are displayed in Eqs. (10.1)–(10.8) (notation as in Figure 10.4): Cooler C3 load: QC3 = 5970 - X

(10.1)

Temperature of stream C1: TC11 = 247 + X /100

(10.2)

Heater H8 load: QH8 = 5300 - X

(10.3)

Exchanger E1 heat load: EE1 = 14700 + X

(10.4)

Temperature 1 of stream H1: TH11 = 190 - X /100

(10.5)

Output temperature of C2: TC2,out = 164

(10.6)

Input temperature of C2: TC2,in = 35

(10.7)

Temperature 1 of stream H1: 99.7  X /100

(10.8)

Answer to (b)(2). The temperature differences should be checked at the affected heat exchangers, which are E1 and E2. As can be seen, the heat capacity flow rate (CP) values for both streams in E1 are equal to 100 kW/°C. Exchanger E2’s hot stream has a higher CP value than that for the cold stream, so the smaller temperature difference will be at its hot end. This allows one to calculate the maximum amount of the load X to shift by solving a few inequalities. For process exchanger E2, the temperature difference should not be less than ΔTmin, and this determines the value of the maximum heat load that can be shifted: TH11 – TC2,out ≥ ∆Tmin

(10.9)

190 – X/100 – 164 ≥ 10

(10.10)

X ≤ 2600 kW

(10.11)

For this value of load shift, the exchanger E2 will be pinched at its hot end as follows: TH11 = 174.0°C and TC2,out = 164.0°C. The temperatures at the cold end will be TH12 = 83.7°C and TC2, in = 35.0°C. Answer to (c)(1). Total heating requirement for the existing network: Σ Q H = Q H8 + Q H9 = 27,700 kW. Total cooling requirement for the network: Σ Q C = Q C3 + Q C6 + Q C10 = 21,345 kW. There is no inappropriate use of utilities. Compared with the targets, both total utility heating and total utility cooling are higher by 9920 kW, which is due to cross-Pinch heat transfer. Answer to (c)(2). The Process Pinch is at 150°C for hot streams and at 140°C for cold streams. Comparing the network temperatures with the Pinch location yields a list of exchangers that violate the Pinch; see Table 10.2.

223

224

Chapter Ten Exchanger

Hot side violation

Cold side violation

E1

No

Yes

E2

Yes

Yes

E4

No

No

E5

Yes

Yes

E7

Yes

No

TABLE 10.2

Exchangers That Violate the Pinch (Problem 1)

Stream

Tin [°C]

Tout [°C]

CP [kW/°C]

1

Cold

38

205

11

2

Cold

66

182

13

3

Cold

93

205

13

4

Hot

249

121

17

5

Hot

305

66

13

TABLE 10.3

Process Stream Data for Problem 2

10.1.2 Heat Pinch Technology: Second Problem Problem 2: Task Assignment The stream data for a process are as listed in Table 10.3. The hot utility is steam at 200°C, the cold utility is water at 38°C, and ΔTmin = 24°C. (a) Plot the Composite Curves (CCs) for this process. (b) Determine Q H,min, QC,min, and the Pinch temperatures. (c) Assuming that the cost of cooling water and steam is 18.13 and 37.78 $ kW−1 y−1, plot the minimum annual cost for the utilities as a function of ΔTmin in the range 51–54°C (in 1° increments). (d) Design a network that features a minimum number of units and maximum energy recovery for ΔTmin = 24°C. Problem 2: Solutions Answer to (a). The Composite Curves for the process stream data are shown in Figure 10.5. Answer to (b). The position of the CCs in Figure 10.5 indicates that, for ΔTmin = 24°C, this is a threshold problem at the cold end: Q H,min = 0 kW. On the cold end there is excess of hot streams, which means that some cold utility is required: Q C,min = 482 kW.

Examples and Case Studies FIGURE 10.5 Composite Curves for Problem 2.

T [°C]

ΔTmin = 24°C

No heating utility

200

100 482 kW 0 0

2000

4000

ΔH [kW]

Utility Cost [$/y] 12000 11000 10000 9000 8000 51

FIGURE 10.6 utility cost.

52

54 ΔTmin [°C]

53

Minimum allowed temperature difference ΔTmin versus annual

ΔTmin [°C] 51

52

53

54

QH [kW]

0

0

27

57

Cost of heating [$/y]

0

0

1,020

2,153

QC [kW]

482

482

509

539

Cost of cooling [$/y]

8,739

8,739

9,228

9,772

Total utility cost [$/y]

8,739

8,739

10,248

11,926

TABLE 10.4

Utility Requirements and Cost for Various ΔTmin Values

Answer to (c). The utility cost plot, which is given in Figure 10.6, is based on the data in Table 10.4. Answer to (d). A network that features the minimum number of units and maximum energy recovery is shown in Figure 10.7.

225

226

Chapter Ten CP [kW/°C]

(a) 121°C

163.4°C

249°C

E4

E1 E2

66°C

103.1°C

C 482 kW

1

305°C

E3

38°C

4

17

CP=9.1 kW/°C

CP=3.9 kW/°C

5

205°C

E2

13

11

1837 kW 2

66°C

121.43°C 182°C E3 E4 720 kW 93°C

3

13

788 kW E1

205°C

13

1456 kW One possible design CP [kW/°C]

(b) E3

E1

121°C

66°C

C

103.1°C

CP=5.22 kW/°C

E2

E4

249°C

CP=11.78 kW/°C

193°C

17 4 305°C

E1

5

13

482 kW 1

38°C

E4

144.3°C

1169 kW 2

66°C

3

205°C

E3 668.16 kW E2

182°C

13

1508 kW

93°C

11

E1

205°C 13

1456 kW A second possible design

FIGURE 10.7

10.2

Optimal Heat Exchanger Network.

Total Sites 10.2.1 Total Sites: First Problem Problem 3: Task Assignment Suppose a Total Site incorporates two processes, A and B. The stream data for process A (assuming ΔTA,min = 10°C) are given in Table 10.5, and the GCC for this process is shown in Figure 10.8. The stream data for process B (assuming ΔTB,min = 10°C) are shown in Table 10.6.

Examples and Case Studies Stream name

Supply temp. [°C]

Target temp. [°C]

ΔH [kW]

A1

50

140

450

A2

100

30

420

A3

100

140

80

TABLE 10.5 Data for Process A (Problem 3)

ΔTmin = 10°C

(330;145)

T* [°C]

150 Sink A1

Sink A2 (59;105)

100

(0;95) Source A1

50 20

Source A2

(40;55)

(220;25) 0

100

200

300

ΔH [kW]

FIGURE 10.8

Grand Composite Curve for process A (Problem 3).

Stream name

Supply temp. [°C]

Target temp. [°C]

CP [kW/°C]

B1

190

120

6

B2

100

240

4

B3

80

60

2

TABLE 10.6

Data for Process B (Problem 3)

High-pressure (HP) steam from a boiler is available at 240°C saturation temperature, and cooling water is available at 20–30°C. It is necessary to analyze these two processes (and hence the Total Site) as follows: (a) Find the Pinch temperatures and minimum utility demands for processes A and B. (b) Construct the GCC for process B.

227

228

Chapter Ten (c) Construct the Total Site Profiles (TSPs). (d) Assuming that the site manager is willing to accept just one more steam main in addition to the HP, identify this steam level on the Site Profiles. What saturation temperature will yield the most energy savings? (e) Determine the load target for this steam level. Problem 3: Solutions Answer to (a). For process A, ΔTmin = 10°C, the minimum hot utility is 330 kW, and the minimum cold utility is 220 kW (see Table 10.7). For process B, ΔTmin = 10oC, the minimum hot utility is 240 kW, and the minimum cold utility is 140 kW (see Table 10.8). Answer to (b). Given the data in Table 10.8, the GCC for process B is drawn as shown in Figure 10.9. Answer to (c). Using the GCC plots from Figures 10.8 and 10.9, the heat source and heat sink segments have been extracted. These segments are listed in Tables 10.9 and 10.10 for process A and process B, respectively. The data reported in Tables 10.9 and 10.10 have been combined into composite heat source and sink profiles. Figures 10.10 and 10.11 illustrate the composition procedure, which is analogous to the one for constructing the process CCs. Figure 10.12 shows the resulting TSPs.

Interval

Temperature [°C]

Enthalpy [kW]

1

145

330

2

105

50

3

95

0 (Pinch)

4

55

40

5

25

220

TABLE 10.7

Interval

Problem Table for Process A (Problem 3(a))

Temperature [°C]

Enthalpy [kW]

1

245

240

2

185

0 (Pinch)

3

115

140

4

105

100

5

75

100

6

55

140

TABLE 10.8

Problem Table for Process B (Problem 3(a))

Examples and Case Studies ΔTmin = 10°C

(240;245)

Sink B1 (0;185) 200 T* [°C]

Source B1 (100;135) (140;115)

(100;105) 100

(100;75)

Source B2 (140;55)

40 0

50

100

150

200

250

ΔH [kW]

FIGURE 10.9

Segment Sink A1

Grand Composite Curve for Process B (Problem 3(b)).

T *start [°C]

T *end [°C]

ΔH [kW]

T **start [°C]

T **end [°C]

280

110

150

105

145

Sink A2

95

105

50

100

110

Source A1

95

55

40

90

50

Source A2

55

25

180

50

20

TABLE 10.9

Heat Source and Sink Segments from the GCC for Process A [Problem 3(c)]

Segment

T *start [°C]

T *end [°C]

ΔH [kW]

T **start [°C]

T **end [°C]

Sink B1

185

245

240

190

250

Source B1

185

135

100

180

130

Source B2

75

55

40

70

50

TABLE 10.10 Heat Source and Sink Segments from the GCC for Process B [Problem 3(c)]

Answers to (d) and( e). By analyzing the TSPs (Figure 10.12), one can see that there is an opportunity to match heat source and heat sink requirements in the steam temperature interval between 100°C and 180°C. The proposed steam saturation temperature is in the interval from 117.1°C to 130°C. Within this interval, the maximum heat recovery through the steam system (equal to 100 kW) is achieved. This results from matching the values for steam generation and steam use (here both are equal to 100 kW).

229

230

Chapter Ten Source Source Source Source A2 B1 B2 A1

TB [°C] 180

ΣCP = 2

ΔH = 100

ΣCP = 0

ΔH = 0

ΣCP = 1

ΔH = 20

ΣCP = 3

ΔH = 60

ΣCP = 6

ΔH = 180

130 90 70 50 20 ΔH [kW]

40

180

100

40

CP [kW/°C]

1

6

2

2

FIGURE 10.10

Combined Site heat sources for Problem 3(c). TB [°C]

FIGURE 10.11 Combined Site heat sinks for Problem 3(c).

Sink A1 Sink A2 Sink B1 250 ΣCP = 4 ΔH = 240 190 ΣCP = 0 ΔH = 0

150

ΣCP = 7 ΔH = 280 110 ΣCP = 5 ΔH = 50 100 ΔH [kW] CP [kW/°C]

280

50

240

7

5

4

Temperature 250 Temperature interval with 100 kW heat recovery via the steam system T

∗∗

T

∗∗

= 130°C

150

= 117.1°C

50

−400

−200

0

200 ΔH [kW]

FIGURE 10.12

Total Site Profiles for Problem 3(c).

400

600

Examples and Case Studies

10.2.2 Total Sites: Second Problem Problem 4: Task Assignment Two processes (A and B) are operating on a site. The stream parameters for process A and process B are given in Tables 10.11 and 10.12, respectively. Medium-pressure (MP) steam from a boiler is available at 220°C saturation temperature, and ΔTmin = 10°C for both processes. The cooling water supply temperature is 18°C and the return temperature is at most 35°C. (a) Use the Problem Table Algorithm (PTA) to identify the minimum heating/cooling duty for each process, and plot the GCCs. (b) Create the TSPs including the GCC pockets. (c) Select the saturation temperature for a second (low-pressure) steam level, and construct the Total Site composites, so as to maximize heat recovery via the steam system. Problem 4: Solutions Answer to (a). Pinch Analysis has been applied to the two processes just described, and the targets thus identified are given in Table 10.13. The GCCs for process A and process B are shown in Figures 10.13 and 10.14, respectively.

Stream

Tsupply [°C]

Ttarget [°C]

CP [MW/°C]

∆H [MW]

160

0.15

2.55

116.01

0.15

6.16

A1

143

A2

75

A3

124

90

0.412

14.0

A4

90

84

0.35

2.1

A5

84

37.5

0.101

4.7

CP [MW/°C]

∆H [MW]

TABLE 10.11

Stream

Stream Data for Process A (Problem 4)

Tsupply [°C]

Ttarget [°C]

158.3

159.9

1.33

B2

70

158.3

0.05

4.42

B3

10

70

0.03

1.8

B4

180

135.6

0.075

3.33

B5

135.6

105

0.105

3.21

B1

TABLE 10.12

Stream Data for Process B (Problem 4)

2.08

231

232

Chapter Ten Q H,min [MW]

Q H,min [MW]

Pinch (hot/cold) [°C]

Process A

2.852

14.955

124 / 114

Process B

1.800

0

None (threshold problem)

TABLE 10.13

Heat Recovery Targets for Problem 4(a)

∗ T [°C]

(2.9; 165.0)

160

(0.3; 148.0)

140

(0.3; 121.0)

120

(8.9; 85.0)

100

(0; 119.0)

(10.3; 79.0)

80

(9.9; 80.0)

60 40 (15.0; 32.5)

20 0 0

FIGURE 10.13

2

4

6

8

10

12

14

ΔH [MW]

GCC for process A [Problem 4(a)].

T* [°C] (1.8; 175.0)

180

(0.5; 163.3)

(2.6; 164.9)

160 140 120

(1.4; 130.6)

100 (3.1; 100.0)

80 (1.8; 75.0)

60 40 20

(0; 15.0)

0 0

FIGURE 10.14

0.5

1

1.5

2

2.5

3

ΔH [MW]

GCC for process B [Problem 4(a)].

Answer to (b). The TSPs for the combination of the two processes are plotted in Figure 10.15. The apparent temperature overlap of the profiles indicates a good opportunity for heat recovery. Answer to (c). The heat recovery on the site can only take place via the steam system. Any steam raised from process cooling has to be utilized to the greatest

Examples and Case Studies extent possible in order to maximize the recovery. Usage may exceed generation; in this case, the difference would be made up by MP steam. The profiles in Figure 10.15 were used to balance steam generation and use by the processes by varying the LP level saturation temperature. This has been achieved for LP generation and use steam loads of 6.9 MW at 109°C saturation temperature, which corresponds to 1.39 bar(a) steam pressure. The Total Site composites are shown in Figure 10.16

T** [°C] 200

100

50

−30

−25

FIGURE 10.15

−20

−15

−10

−5

0 5 ΔH [MW]

10

15

20

10

15

20

Total Site Profiles for Problem 4(b).

T** [°C] 200

6.9 MW 100

50

−30

−25

FIGURE 10.16

−20

−15

−10

−5

0 5 ΔH [MW]

Total Site composites for Problem 4(c).

233

234 10.3

Chapter Ten

Integrated Placement of Processing Units and Data Extraction Problem 5: Task Assignment The process flow sheet for a base-case design is shown in Figure 10.17 with some additional data. The CCs and GCC of the process (with appropriate data) for ΔTmin = 20°C are shown in Figures 10.18 and 10.19, respectively. purge FR

H

120°C

m=0.4

900

C m=1 F1 F2

1300

505

50°C

180°C

CA

130°C

H 50°C

180°C

R1 T=180°C

180°C

m=0.8

220°C

A

H

HM m=1.4

220°C RA

1050

H CB 200°C

P2

200°C

70°C

980

Column A

1000

C

B

m=1.3 Column B

RB

C

Heat exchanged with cold utility

H

Heat exchanged with hot utility

Q

Heat exchanged [kW]

1928

m=0.5 70°C P1

C

FIGURE 10.17

150°C

270°C

H

Process flowsheet for the base-case design (Problem 5).

ΔTmin = 20 °C

T [°C]

m=[kg/s] 270°C

250

2642.6

Pinch

200

Th = 240 °C Tc = 220 °C

150 100 50

10316.6

1958.6 0 0

FIGURE 10.18

2000

4000

6000

8000

10000 ΔH [kW]

Composite Curves for the process in Problem 5.

Examples and Case Studies T (°C)

250 200 150 100 50 0 0

500

FIGURE 10.19

1000

1500

2000

2500

Q (kW)

GCC for the process in Problem 5.

(a) Extract the appropriate stream data for performing a Pinch Analysis. Tabulate the extracted data where appropriate. If a stream involves phase changes (several segments), then give the relevant details (e.g., stream F1 has three segments: liquid phase, vaporization, and vapor phase). (b) In the base-case design, what is the hot and cold utility consumption and how much is the process heat recovery? Compare the utility usage in the base case with the targets shown on the CCs. Why are they different? (c) Explain how the heat recovery system can be improved over the base case without modifying any conditions (e.g., reactor pressure, column pressure) of the main process. (d) Refer to the GCC in Figure 10.19. (1) If a heat pump is proposed, what operating temperature levels will best fit the heating and cooling needs of the process? (2) What qualitative suggestions can be made concerning alternatives for utility saving and appropriate utility placement? (e) If process modifications are allowed, comment on whether they could help to improve the process Heat Integration. Your answer should address the reactors, the distillation columns, feed vaporization, and soft data. For this problem, the following assumptions are made. Utilities generated can be sold, and the unit cost of high-temperature utilities

235

236

Chapter Ten is greater than that for low-temperature utilities. The temperature of flue gas for direct heating ranges from 800°C to 160°C. Steam usage and generation are isothermal utilities (up to four levels between 100°C and 340°C). A heat pump or heat engine can be introduced. Additional data for the problem: • Condensers and reboilers of distillation columns A and B involve only phase changes. • In the condenser of distillation column B, total condensation is assumed (i.e., the outlet is in the liquid phase only). • An endothermic reaction takes place in reactor R1. A heating medium (HM) is necessary to keep the isothermal condition in R1. Some properties of the streams are as follows: F1:

Boiling point = 120°C, ΔHvap = 990 kJ/kg, Cp,vap = 4.5 kJ/kg·°C

F2:

Boiling point = 125°C, ΔHvap = 1250 kJ/kg, Cp,vap = 7.5 kJ/kg·°C, Cp,liq = 15 kJ/kg·°C

Cp,vap = 5.0 kJ/kg·°C HM: Cp,liq = 25 kJ/kg·°C

FR: P1:

Boiling point = 270°C, ΔHvap = 1556 kJ/kg

P2:

Boiling point = 200°C

Problem 5: Solutions Answer to (a). Stream data needed to perform a Pinch Analysis is reported in Table 10.14. Answer to (b). For the base case, Q H = 4828 kW, Q C = 3366.4 kW, and process heat recovery = 3530 kW. The targets are Q H = 2642.6 kW and Q C = 1958.6 kW, and process heat recovery = 5715.8 kW. The base-case design requires much more utility consumption. This is because some heat is transferred across the Pinch and also because there is some unnecessary utility use. For example, some amount of heat is needed in the column B reboiler for heating up P1, and this amount must be taken out again when P1 needs cooling. Answer to (c). • The cold streams below the Pinch are F1, F2, and FR. These streams can be heated up by P1 (parts below the Pinch), P2, and by the condensers of columns A and B. In the base case, stream P1 is used to supply heat to stream F2, resulting in heat transfer across the Pinch. Instead, to heat up stream F2 at its higher temperature range, heat exchange with stream P2 can be employed; for the lower-temperature part of F2, the heat from the condenser of column A can be recovered. • Above the Pinch, P1 can be used to heat up parts of the column A reboiler or of the heating media of reactor R1.

Examples and Case Studies Stream

Type

Ts [°C]

Tt [°C]

m Cp ΔHvap [kg/s] [kJ/kg·°C] [kJ/kg]

CP ΔH [kW/°C] [kW]

F1-liq F1-evap F1-vap

Cold Сold Сold

50 120 120

120 120 180

1 1 1

11 — 4.5

— 990 —

F2-liq F2-evap F2-vap

Cold Cold Cold

50 125 125

125 125 180

0.8 0.8 0.8

15 — 7.5

— 1250 —

12 — 6

900 1000 330

HM

Cold

220

250

1.4

25

—

35

1050

CA

Hot

120

120

—

—

—

—

900

11 — 4.5

770 990 270

RA

Cold

220

220

—

—

—

—

1000

FR

Cold

120

180

0.4

5

—

2

120

CB

Hot

200

200

—

—

—

—

980

RB

Cold

270

270

—

—

—

—

1928

P1-cond P1-liq P2

Hot Hot Hot

270 270 200

270 70 70

0.5 0.5 0.8

TABLE 10.14

— 37.17 12.5

1556 — —

— 18.58 10

778 3716 1300

Stream Data for Pinch Analysis [Problem 5(a)].

Answer to (d)(1). Using the GCC in Figure 10.19, from the viewpoint of a heat pump, two good candidates for its integration are as follows: • Across the Process Pinch. Heat rejection from the heat pump to the process T* = 230°C (real temperature T = 240°C) and heat absorption from the process at T* = 190°C (T = 180°C), would result in temperature lift ΔTlift = 60°C. The main challenge is that the heat available for absorption by the heat pump is relatively smaller than what can be delivered by the heat pump above the Process Pinch. • Across a potential Utility Pinch. Heat rejection level T* = 130°C and absorbtion heat level T* = 110°C. The corresponding real heat pump temperatures are: heat rejection level T = 140°C and heat absorption level, T = 100°C. This results in temperature lift ΔTlift = 40°C. At this level, a large amount of heat is available to be absorbed from the process and an even larger amount can be rejected to the process. Answer to (d)(2). • From the GCC, the heat pump integration can be placed at the levels of 140°C and 100°C with only a small amount of shaft work required. This could save a large part of the cold utility required. • Above the Pinch, a large and quite flat pocket is present in the CCC, providing an opportunity to generate steam at the maximum level of 180°C. • Above the Pinch, steam is preferred over flue gas for a hot utility because the process stream temperatures are not too high.

237

238

Chapter Ten • A heat engine could also be a candidate for the pocket in the GCC below the Pinch. However, since ΔT is small—about 80°C, or [(190 + 10) – (130 – 10)]—only a small amount of work may be produced. Answer to (e). • Reactors. The reaction is endothermic and, to save utility, its heating medium heat demand should be placed below the Pinch. It is now placed above the Pinch. If the pressure and temperature of reactor R1 are reduced, then an alternative heating media with lower temperature levels could be used. As a result of decreased R1 pressure, the boiling points of feeds F1 and F2 would also decrease. This would result in different targets. For instance the GCC could be shifted more to the left and the Pinch point could be changed, resulting in more process heat recovery. • Distillation columns. The reboilers of columns A and B currently evaporate the entire flow from the column bases. The appropriate arrangement would be to move the reboilers to evaporate only the branches of these flows that are intended for the columns. • Feed vaporization. In the base case, the vaporization of F1 and F2 are both placed below the Pinch. However, as mentioned, the current vaporization of F2 results in cross-Pinch heat transfer. Also, the vaporization of F1 employs utility heating below the Pinch, which should be eliminated and substituted for process-to-process heat recovery. • Soft data. The P1 and P2 target temperatures are soft data that can be changed. The temperatures could be increased to reduce cold utility required, but this would not change the CC much.

10.4 Utility Placement 10.4.1

Utility Placement: First Problem

Problem 6: Task Assignment A set of data for a part of a crude distillation process has been extracted, and the stream data are shown in Table 10.15. For this problem, the minimum temperature difference is ΔTmin = 10°C. The available utilities are presented in Table 10.16. A targeting procedure was performed for the initial data summarized in Tables 10.15 and 10.16. Figure 10.20, which exhibits two Pinch points, shows the balanced CCs for the problem. (a) Complete the missing entries in Table 10.15. (b) Identify the Pinches and explain their significance. (c) Draw the design grid for the problem, including the hot utilities. Position the streams relative to the location of the Pinches. (d) Design the MER HEN below the Process Pinch. (e) Design the MER HEN above the Process Pinch. (f) Design the MER HEN above the Utility Pinch.

Examples and Case Studies Stream

Name

Ts [°C]

1

OH_Naphta_1

100

41

27.5113

2

OH_Naphta_2

132

60

23.1850

3

OH_HKD

224

65

4

LCT

268

30

5

Residue

283

45

336.25

1.4128

6

Crude

30

146

2031.50

17.5132

7

Denaphta_1

117

204

977.88

8

Denaphta_2

176

305

1641.45

TABLE 10.15

Tt [°C]

ΔH [kW]

CP [kW/°C]

11.2400 363.12

1.5257

12.7244

Process Streams for Problem 6

Stream

Ts [°C]

Tt [°C]

Cost [£/kWy]

HP steam

320.1

320.0

100

MP steam

260.1

260

60

20.0

40.0

8

Cooling water TABLE 10.16

Available Utilities for Problem 6

HP steam = 654.2 kW 320.0°C MP steam = 874.4 kW

300

320.1°C 305.0°C

260.1°C 260.0°C 250.1°C

T* [°C]

224.0°C 200

204.0°C 176.0°C 132.0°C 100.0°C

100 C .0° 60.0°C

5 41.0°C 4

30.0°C 0

20.0°C

146.0°C 122.0°C

40.0°C Cooling water = 2657 kW 2000

4000

6000

8000

ΔH [kW]

FIGURE 10.20 Problem 6.

Balanced Composite Curves and heat recovery targets for

239

Chapter Ten Problem 6: Solutions Answer to (a). Table 10.17 shows the missing parameters of process streams described in Table 10.15. Answer to (b). There are two Pinches: the Process Pinch (located at 132°C/122°C) and the Utility Pinch (located at 260.1°C/250.1°C; see Figure 10.21. The Utility Pinch is caused by the placement of the MP steam. More significant is the Process Pinch, which divides the design area into two different parts: a net heat sink above the Pinch temperatures and a net heat source below the Pinch temperatures. The Utility Pinch further subdivides the area above the Process Pinch. In the interval between the Process Pinch and the Utility Pinch, the only utility allowed is the MP steam. Above the Utility Pinch, the only utility available remains the HP steam. Answer to (c). See Figure 10.22.

No

Name

Ts [°C]

1

OH_Naphta_1

100

41

1623.17

27.5113

2

OH_Naphta_2

132

60

1669.32

23.1850

Tt [°C]

ΔH [kW]

CP [kW/°C]

3

OH_HKD

224

65

1787.16

11.2400

4

LCT

268

30

363.12

1.5257

5

Residue

283

45

336.25

1.4128

6

Crude

30

146

2031.50

17.5132

7

Denaphta_1

117

204

977.88

11.2400

8

Denaphta_2

176

305

1641.45

12.7244

TABLE 10.17

Process Streams for Problem 6(a) with Missing Data Filled In

HP steam = 654.2 kW MP steam = 874.4 kW

300

260.0°C

320.0°C

200 132.0°C

Utility Pinch

5 41.0°C 4

C 60.0°C

30.0°C

20.0°C

204.0°C 176.0°C

Process Pinch

.0°

0

250.1°C

146.0°C 122.0°C

100.0°C

100

Cooling water = 2657 kW 2000

4000

6000

ΔH [kW]

FIGURE 10.21

320.1°C 305.0°C

260.1°C

224.0°C

T [°C]

240

Pinch identification for Problem 6(b), ΔTmin = 10°C.

8000

Examples and Case Studies 132.0°

260.1°

320.1°

320.0°

MP_steam

11

ΔH = 874.373

1

ΔH = 1623.167

CP = 27.51

OH_Nafta_1

132.0°

60.0° CP = 23.18

OH_Nafta_2

2

ΔH = 1669.32

224.0°

65.0° CP = 11.24 ΔH = 753.08

ΔH = 1034.08

CP = 11.24

OH_HKD

3 268.0°

30.0° CP = 1.63

ΔH = 165.621

ΔH = 195.442

CP = 1.63

CP = 1.53

ΔH = 12.053

ΔH = 122.913

CP = 1.41

ΔH = 180.979

CP = 1.41

LCT

CP = 1.41

ΔH = 32.353

5

Residue

146.0°

30.0°

6

4

283.0°

45.0°

CP = 17.51 ΔH = 1611.214 117.0°

CP = 17.51

ΔH = 420.316 204.0°

CP = 11.24

ΔH = 921.68

7 ΔH = 56.2

CP = 11.24

Crude Denafta_1 305.0°

8

ΔH = 942.878

CP = 12.72

Denafta_2

ΔH = 698.589

CP = 12.72

40.0°

20.0°

9

HP_steam

260.1°

CP = 8743.73

100.0°

41.0°

10

ΔH = 654.163

CP = 6541.63 260.0°

Cooling water

CP = 132.83 ΔH = 2656.687 250.1°

122.0°

ΔTmin = 10°C; All temperatures are in [°C], ΔH are in [kW], CP are in [kW/°C]

FIGURE 10.22

Preliminary grid diagram for Problem 6(c).

Answer to (d). See Figure 10.23. 1623.17 kW

132.0°

100.0°

41.0°

C1

1 57.71 kW

60.0°

132.0°

62.51°

2

2

C3 696.88 kW 65.0° C5

127.3°

132.0° 3

4

155.62 kW 30.0°

132.0°

C6

4

122.91 kW 132.0°

45.0°

5

C7 30.0° 2

6

122.0°

1611.21 kW 7

117.0°

4

122.0°

56.2 kW 20.0° 9

C1

C7

C6

C5

C3 122.0°

FIGURE 10.23

HEN design below the Process Pinch [Problem 6(d)].

241

242

Chapter Ten Answer to (e). See Figure 10.24. 260.1°

132.0°

260.0°

12

214.0° CP = 11.24

8

9

CP = 1.53

224.0°

13

260.1°

11

3 4

10

5

11

CP = 1.41 CP = 8.755

10

CP = 17.51

6

CP = 11.24

7

144.32° 143.49°

142.67° 195.44 kW

11

146.04° 13

180.98 kW

43.90 kW 8

921.68 kW 8

CP = 12.72

176.0°

204.0°

185.32° 12

9

112.4 kW

830.48 kW

122.0°

250.1° All temperatures are in [°C], ΔH is in [kW], CP is in [kW/°C]

FIGURE 10.24

HEN design above the Process Pinch [Problem 6(e)].

Answer to (f). See Figure 10.25. 260.1° 320.0°

16

320.1°

CP = 6541.86 12.05 kW

268.0°

15

4

CP = 1.53 283.0° 14

CP = 1.41

CP = 3.36

8

14

15

251.99°

255.19° 253.59°

CP = 3.36 32.35 kW

5

16

305.0°

CP = 6.72 654.16 kW

250.1°

FIGURE 10.25

MP steam

HEN design above the Utility Pinch [Problem 6(f)].

10

Examples and Case Studies

10.4.2

Utility Placement: Second Problem

Problem 7: Task Assignment A process involves the set of process streams described in Table 10.18. The utilities available to satisfy its heating and cooling requirements are given in Table 10.19. For the HEN to be designed, assume ΔTmin = 30°C. (a) Identify the minimum heating duty, the minimum cooling duty, and the Process Pinch location. (b) Plot the GCC. (c) Perform an appropriate placement of the utilities against the GCC so as to achieve minimum total cost of the utilities. (1) Draft the placement on the GCC. (2) Calculate the total duty for each of the utilities. (3) Calculate the total utility cost for the problem. (d) Consider the following ways to reduce the utility costs further, and comment on their suitability for application to

Stream H1

Ts [°C]

Tt [°C]

CP [MW/°C]

175

75

3.5

H2

100

40

2.4

H3

180

130

1.5

H4

195.1

195

100

C1

50

C2

140

C3

80

140

1.5

C4

20

80

3.0

TABLE 10.18

ΔH [MW]

150

2.0

140.1

150

Process Streams Data for Problem 7

Name

Ts [°C]

Tt [°C]

HP steam

300.1

300

65000

MP steam

200.1

200

50000

Cooling water

15.0

20.0

7000

Chilled water

5.0

10.0

30000

TABLE 10.19

Utilities Available for Problem 7

Cost [$/MWy]

243

244

Chapter Ten this current problem. Wherever appropriate, suggest how an option can be exploited. (1) Flue gas heating (2) Heat pumping (3) Introduction of a new steam level Problem 7: Solutions Answer to (a). The heat recovery targets and the Pinch location can be obtained with the help of the PTA. The heat cascade intervals and the corresponding stream population are shown in Table 10.20, and the computed problem table is given in Table 10.21.

Temperature boundary

Interval number

Stream population

180.1 1

H4

180.0 2 165.0 3

H3, C1

3

H1, H3, C1

4

H1, H3, C1, C2

5

H1, H3, C1, C3

6

H1, C1, C3

7

H1, C1, C4

8

H1, H2, C1, C4

9

H1, H2, C4

160.0 155.1 155.0 115 95.0 85.0 65.0 60.0 10

H2, C4

11

H2

35.0 25.0 TABLE 10.20 Heat Cascade Intervals and Stream Population for Problem 7(a)

Examples and Case Studies Alternatively, the heat recovery targets can be obtained by plotting the CCs, as shown in Figure 10.26. Answer to (b). See Figure 10.27. Answer to (c)(1) and (c)(2). See Figure 10.28. Answer to (c)(3). Total utility cost = 37.5 [MW MP steam] × 50,000 [$/MWy] + 62.5 [MW cooling water] × 7,000 [$/MWy] + 24 [MW chilled water] × 30,000 [$/MWy] = 3,032,500 [$/y]

Interval number

Temperature [°C]

1

180.1

2

180

Enthalpy [MW] 37.5 137.5

3

165

137.5

4

160

135.0

5

155.1

149.7

6 (Pinch)

155

0.0

7

115

60.0

8

95

60.0

9

85

45.0

10

65

63.0

11

60

77.5

12

35

62.5

13

25

86.5

TABLE 10.21

Problem Table for Problem 7(a)

FIGURE 10.26 T [°C] Composite Curves for 250 Problem 7(a), ΔTmin = 30°C.

QH,min = 37.5 MW

200 150 Pinch: 170°C (hot) 140°C (cold)

100 50

QCmin=86.5 MW 0 0

200

400

600

800

ΔH [MW]

245

246

Chapter Ten FIGURE 10.27 Grand Composite Curve for Problem 7(b), ΔTmin = 30°C.

QH,min = 37.5 MW T [°C] 150 100 50 QCmin=86.5 MW 0 0

FIGURE 10.28 Appropriate placement of utilities for Problem 7(c).

50

T [°C]

100

ΔH [MW]

MP steam 37.5 MW

150 100 Cooling Water 62.5 MW

50

Chilled Water 24 MW

0 0

50

100

ΔH [MW]

Answer to (d)(1). The flue gas heating option will probably be more expensive than heating with steam. The temperature levels in the problem do not suggest exploitation of furnace heat. Answer to (d)(2). The appropriate placement of a heat pump is across the Process Pinch, so the pump will transfer heat from below to above the Pinch. In this problem it is technically impractical to install a heat pump with water or steam as a working fluid, since this would require operation at a slight vacuum (the Pinch is at 170°C/140°C). The relatively small duties that could be achieved with this technique indicate that investment in a heat pump here is likely to be economically unattractive. Answer to (d)(3). Introducing a new steam level at a steam temperature of 165°C is a good option that can be exploited by passing the steam (taken at 200°C) through a steam turbine. This has the potential of generating additional power on the site. The steam would be returned to the process at the level of 165°C (the process heating requirement is at 150°C, which makes this arrangement feasible). If the site could use additional power, then this option may reduce the overall utility cost by providing on-site power generation.

Examples and Case Studies

10.5 Water Pinch Technology 10.5.1 Water Pinch Technology: First Problem Problem 8: Task Assignment A certain process contains several water-processing operations, as shown in Table 10.22. (a) Create the limiting CCs by plotting the contaminant concentration, C, against contaminant load, m [kg/h], [ppm]. (b) Calculate the minimum water flow rate for maximum reuse. Problem 8: Solutions Answer to (a). The individual limiting water profiles are graphed in Figure 10.29. Figure 10.30 shows the result when these water profiles are combined.

Operation

Contaminant flow rate [kg/h]

1

Cin [ppm] Cout [ppm]

2

0

2

5

3

30

4

4

TABLE 10.22

Limiting flow rate [t/h]

100

20

50

100

100

50

800

40

400

800

10

Data for Water-Processing Operation of Problem 8

800

C [ppm]

4

400 3

100 1 50 0 2

2 7

37 41 m [kg/h]

FIGURE 10.29

Limiting water profiles for Problem 8(a).

40

247

Chapter Ten Answer to (b). The minimum wastewater is targeted as follows: Minimum flow rate

Mass pickup at pinch Pinch concentration 9 [kg/h] 9 ˜ 10 6 ª kg º 100 [ppm] 100 «¬ h »¼ 9 ˜ 10 3 100

ªtº «¬ h »¼

90 [t/h]

See Figure 10.31.

FIGURE 10.30

Combined limiting water profiles for Problem 8(a).

800

C [ppm]

248

400 ine /h) t ly L upp ate 90 S r r e t w Wa m flo imu n i (M

Pinch

100

0

1

9

21 m [kg/h]

FIGURE 10.31

Minimum wastewater targeting for Problem 8(b).

41

Minimize flowrate

Examples and Case Studies

10.5.2 Water Pinch Technology: Second Problem Problem 9: Task Assignment Using the stream data from Problem 8, suggest a design of a network for maximum reuse of water. The limiting CC is shown in Figure 10.32. Problem 9: Solution Cut off the pockets of the limiting CC. The minimum water requirement for each pocket can then be defined for each region (Figure 10.33). This enables one to propose the design strategy shown in Figure 10.34. Following the design strategy, set up a design grid as shown in Figure 10.35. Connect streams to water mains and merge operations that cross boundaries; see Figure 10.36. Remove intermediate water mains where this is appropriate (Figure 10.37). Then connect operations directly, as shown in Figure 10.38. Finally, Figure 10.39 illustrates (in conventional flowsheet form) one of the possible resulting designs of the water system.

C [ppm]

800

400

100

0

1

9

21 m [kg/h]

FIGURE 10.32

Limiting Composite Curve for Problem 9.

41

249

Chapter Ten

C [ppm]

800

45.7 t/h

400

100 50 90 t/h

m [kg/h]

FIGURE 10.33 Water Pinch diagram used to target the minimum water flow rate in Problem 9.

800

C [ppm]

250

45.7 t/h 800 ppm

400 100 50

90 t/h

FIGURE 10.34

90 t/h

45.7 t/h 100 ppm 44.3 t/h100 ppm

m [kg/h]

Design strategy for Problem 9.

Examples and Case Studies Flowrate required for the interval

1

20 t/h

Limiting Flowrates

100 t/h

2 50 ppm

40 t/h

3 50 ppm

3

10 t/h Wastewater

0 t/h 800 ppm

45.7 t/h 100 ppm

90 t/h F.W.

(90-90) 0 t/h

(90-45.7) 44.3 t/h 100 ppm

4 400 ppm

(45.7-0) 45.7 t/h 800 ppm

Water mains

FIGURE 10.35

Design grid for the water system in Problem 9.

90 t/h F.W. 20 t/h

1

45.7 t/h 100 ppm 20 t/h 50 t/h

100 t/h

20 t/h

40 t/h

0 t/h 800 ppm

2 3

40 t/h 20 t/h 5.7 t/h

10 t/h 0 t/h

FIGURE 10.36

44.3 t/h

4 45.7 t/h

Streams are connected with the water mains (Problem 9).

251

252

Chapter Ten 90 t/h F.W. 20 t/h

45.7 t/h 100 ppm

0 t/h 800 ppm

20 t/h

1

50 t/h

100 t/h

20 t/h

40 t/h

2 3

40 t/h 20 t/h 5.7 t/h

10 t/h 0 t/h

4

44.3 t/h

45.7 t/h

FIGURE 10.37 Removing intermediate water mains and then connecting sources and sinks (Problem 9).

90 t/h F.W. 20 t/h

20 t/h

1

50 t/h

100 t/h

20 t/h 40 t/h

2 3 20 t/h

5.7 t/h

10 t/h 0 t/h

FIGURE 10.38

4

44.3 t/h

45.7 t/h

Connecting operations directly (Problem 9).

20 t/h 20 t/h F.W. 90 t/h

50 t/h

Operation 1

Operation 2

40 t/h

5.7 t/h

Operation 3 Wastewater 90 t/h Operation 4 44.3 t/h

FIGURE 10.39

Flowsheet representation of a water system design (Problem 9).

CHAPTER

11

Industrial Applications and Case Studies

T

his chapter provides an overview of selected implementations of the Process Integration methodology for various industrial case studies. The presentation is somewhat condensed because of space limitations; more information is available in the works cited.

11.1

Energy Recovery from an FCC Unit In this case study, the Heat Exchanger Network (HEN) of a Fluid Catalytic Cracking (FCC) unit process consisted of a main column and a gas concentration section (Al Riyami, Klemeš, and Perry, 2001). The stream data was made up of 23 hot streams and 11 cold streams. The associated cost and economic data required for the analysis were specified by the refinery owners. Incremental area efficiency was used for the targeting stage of the retrofit design. This was carried out using the Network Pinch method (Asante, 1996; Asante and Zhu, 1997), which consists of a diagnosis stage and an optimization stage. In the diagnosis stage, a few promising retrofit steps were generated using the UMIST (now the University of Manchester) software package SPRINT (2009). This software was also used to optimize the initial design by trading off capital cost against energy savings. The design options were then compared and evaluated, followed by the final retrofit design proposed for final inspection. The existing ΔTmin of the process was identified as 24°C, and the hot utility consumption of the process was 46.055 MW; the area efficiency of the existing design was 0.805. The potential for energy saving was then derived from the resultant Composite Curves, which are shown in Figure 11.1. As seen in the figure, the Composite Curves are relatively wide apart except in the area around the Pinch. The capital cost was estimated under the assumption that the retrofit distribution of area would be the same as that for the existing network. The resulting optimum minimum temperature approach was found to be about 11.5°C for incremental α and about

253

Chapter Eleven 400 ΔTmin = 11.50°C Temperature [°C]

254

300

200

100

0

1

2

Enthalpy [MW]

FIGURE 11.1 Composite Curves of FCC process with optimum ΔTmin (after Al Riyami, Klemeš, and Perry, 2001).

17.5°C for constant α. The area efficiency α of the existing network was found to be 0.804. This value indicated that the existing design was using the area reasonably efficiently. Even so, there was still room for improvement. Since the constant-α targeting produced a conservative estimate, an incremental α value of 1.0 was used to set the retrofit target, which yielded potential for energy savings of about 12.117 MW. Analysis of the existing design revealed that there were four process-to-process heat exchangers that transferred heat across the Process Pinch (from above to below the Pinch). It was also found that some heaters supplied utility heat to process streams below the Pinch and that some coolers removed heat from process streams above the Pinch. These energy violations of the established Pinch rules generated the scope of the project’s possible energy savings. The retrofit design using the Network Pinch method allowed a limit to be set on the structure’s energy recovery. The next stage consisted of testing a set of modifications that would result in higher levels of energy recovery in the process. The increase in energy recovery would come at the expense of increased heat exchange area. Therefore, any benefit in energy cost reduction had to be weighed against the additional capital cost associated with increasing that area. A number of promising design solutions were generated, which were then optimized for minimum total cost. The four designs identified each involved a payback period of less than two years, yet increases in energy prices rendered the actual payback period closer to one year. The final design chosen for the retrofit situation was the one with the shortest payback period and the least additional area required; it is shown in Figure 11.2. In this design option, four new heat exchangers were added and one existing exchanger (number 1 in Figure 11.2) was removed, since its duty approached zero. In reality the exchanger equipment item

Industrial Applications and Case Studies 4 5

224° C

238°

293° 12

C 38° C 50° C 108°

38° 38° 38° 38° 38° 46°

C C

38°

C C C

38°

109°

C2

210.5°

7

H5 H6 H7

104° 294.25 kW

83.3° 40

12459 kW

97.17° 62.87°

H8 H9

68.11°

44

H10 63.11° H11 52.5° H12 51.5° H13 96.41°

H14

53267 kW 46° 359.6 kW 48.92° C 563 kW 653.3 kW

96.3°

74.3° 11

193°

9

53° 46°

195.83 kW

46.44°

H19

H21 60° H22

206 kW

102°

C

110°

88.2°

60°

40 3802 kW

H23

134.8°

2

10

171.7° H 385° 22841 kW 4282.8 kW 195° 4

3

2381 kW 1803 kW

5

192.6°

3697.5 kW

8

38°

H18

67.24°

7336 kW

38°

H17

H20

32.3 kW

C

100°

H15 H16

53°

C3

10198.9 kW

55° 50°

1413.6 kW

C5 C6

H4

158°

856.4 kW

C

H3

224°

2

58.32°

C4

238°

41

1235 kW

1815.6 kW C1

207.8° 8

C C

38°

1247 kW

74°

14125 kW

38° 60°

10

3324 kW 62.05° C C 1902 kW 2704 kW C 244.5 kW C 73.9 kW

C

38°

54.9°

C

C

46°

481 kW

293° 43

42

38° 38°

H2

3

760.5 kW 123°

H1

366°

150.8°

52°

40°

366°

6

60°

11

8787 kW 193° 12

872.25 kW

184.5°

6 C7 C8 C9 C10 C11

78.56°

9

118.4° 118° 48.23°

7

43

101.7°

41479.7 kW

4258.8 kW 213.7 kW

119.3°

13291 kW 124° 41 H

2402.6 kW

1151.8 kW

49.68°

44 1051.9 kW

51.16° 95.40°

95°

101.78°

54.3° 763.9 kW

42 5669.4 kW

H 102° H

200 kW

FIGURE 11.2 Grid diagram of the chosen retrofit option (after Al Riyami, Klemeš, and Perry, 2001). Exchanger number 1 from the original network is removed and now used repiped as new added area (exchanger number 42); exchanger number 10 is only repiped.

need not be removed. Instead, it could be used in place of one of the additional exchangers called for by the new design by repiping either the hot or cold stream (so in this case, exchanger number 1 becomes exchanger 42 in Figure 11.2), thus further reducing the additional area

255

256

Chapter Eleven required. All the modifications carried out in the diagnosis stage had the effect of moving heat from below to above the Network Pinch. The final retrofit design produced energy savings of 8.955 MW, about 74 percent of the potential of the design. The annual utility cost savings amounted to $2,388,600, a 27 percent decrease in the utility bill. Since the modified HEN required an investment of $3,758,420, the payback period was less than 19 months. The study demonstrated that a combination of targeting and Pinch Technology (process Pinch and Network Pinch) can yield substantial improvements in an existing HEN and thereby reduce the total network cost. The employed method can recognize bottlenecks in an existing system, and then generate a series of potential improvements by searching for modifications capable of shifting heat from below to above the Network Pinch. It was found that targeting for maximum energy savings at each potential modification usually produces a good trade-off between area and energy cost.

11.2 De-bottlenecking a Heat-Integrated Crude-Oil Distillation System A crude-oil preheating system retrofit problem was studied by Seikova, Varbanov, and Ivanova (1999). The objective of the study was to develop a topology modification proposal for the refinery owners that would feature better energy efficiency than the existing network under a flexibility requirement—namely, that the distillation plant be able to work with several alternative feedstocks. The preheating system of the distillation plant was analyzed, and several topology modifications were evaluated. The retrofit aspect of Heat Integration was first considered systematically by Tjoe and Linnhoff (1986), who proposed a framework for retrofit assessment and targeting. Later, Asante and Zhu (1997) developed the Network Pinch methodology. This hybrid approach, which combines heuristics and Mathematical Programming (MPR), was implemented through an iterative procedure whose two main stages are to identify the heat transfer bottleneck of the given HEN and then to implement modifications for overcoming it. Another important Process Integration issue involves accounting for different plant operating conditions stemming from the market availability of various feedstocks. The case study reported in Saboo, Morari, and Woodcock (1985) was based on the HEN retrofit methodologies just described and combined the energy recovery improvement with handling of the flexibility requirements that are common to real-life processing plants. The crude-oil distillation unit (Figure 11.3) consists of a main distillation column (with 6 m3/h capacity) for fractionating crude oil into four products: light distillate, heavy gasoline, diesel fuel, and atmospheric residue. The preheating HEN recovers heat from the

Industrial Applications and Case Studies

Gases

Water Steam

Light Distillate

Steam

Crude Oil

Steam Atmospheric residue

Diesel Oil

Lower pumparound Heavy Distillate

FIGURE 11.3

Flowsheet of the crude-oil distillation unit.

pump-around and from some of the products before the furnace. To bring the final crude oil temperature to the column’s required target, the remaining heat duty is provided by the combustion of noncondensed light gases and of additional natural gas. The process features the following characteristics: (1) temperaturedependent heat capacities; (2) continuous partial phase change of the crude oil; (3) temperature variations, which are small owing to specifications of the distillation process; and (4) large variations of the hot stream flow rates due to changing stockfeed composition. The three utility sources available for HEN operation are light gases (as a furnace fuel for higher temperature levels), steam at 1 atm (1.01325 bar), and cooling water at 18–35°C. The data used to estimate the utility cost are $68.74/kWy for furnace heating, $103.10/kWy for steam, and $30.00/kWy for cooling water. The following area cost law was used: Capital cost [$ = 25,000 + 680 Area0.81 [m2]

(11.1)

The plant processes a range of alternative feedstocks. Three crude-oil types were selected to represent this range. Feed 1 is a light crude oil; it contains a significant amount of the lightest fractions, which require a large amount of cooling in the condensers. However, the relatively small amount of the heavy fraction means that less reboiler heating is required. Feed 2 is medium crude oil and feed 3 is heavy crude oil. These two feedstocks are characterized by a relatively greater amount of the heavy fractions (diesel and atmospheric residue), which means that more heat is available for recovery in the higher temperature range. It was assumed that, over a year’s worth of operation, the plant uses equal amounts of the three feedstocks. Each alternative feedstock is associated with a unique operating point.

257

258

Chapter Eleven At all three operating points, the crude oil is preheated within a large temperature interval—from 20°C to 310°C. The preheating process consists of three phases. In the first phase, the crude oil is heated from the starting temperature to its bubble point. The next phase involves continuous partial evaporation in heat exchangers. The third and hottest phase is heating to the specified column entry temperature of 310°C (this heating is performed in the furnace). The upper pump-around features a large enthalpy change split between condensation and subcooling segments. None of the other process streams has phase transitions. The existing HEN for the preheating train is shown in Figure 11.4. In order to initialize the retrofit procedure, a Pinch Analysis of the stream data for ΔTmin = 10°C was carried out. The results of this analysis are given in Table 11.1. For the first two feeds, the Pinch is located at the temperature boundary of the crude oil bubble point. For feed 3, the Pinch is located at a temperature that is close to the beginning of the phase change. Note that each operating point offers a different potential for heat recovery. After looking at the existing network and thermodynamic targets, one can suggest several retrofit modifications. First, the hot utility usage below the Pinch leads to extremely poor heat recovery as well as to substantially increased utility cooling and thus to using considerable amounts (30–38 m3/h) of cooling water. Taking a look at the coolers in the temperature interval of heater H1 (Figure 11.4), one can see that the sum of the cooler loads at the outlets of streams H3, H4, and H5 offers enough heat supply to satisfy the heating demand in the interval from 20°C to 60°C. This analysis implies that steam heating can be eliminated through repiping of the coolers as recovery matches. It can also be seen that the availability of heat recovery varies in response to the different temperature levels characteristic of each type of crude-oil feed. This effect is most significant for the atmospheric residue stream H5, whose heat capacity flow rate varies from 0.98 to 1.47 kW/°C. To handle this variation in heat availability temperatures, a cascade of recovery

Feed 1

Pinch location [°C]

Minimum hot utility [kW]

Minimum cold utility [kW]

110–120

556.25

560.26

Maximum heat recovery [kW] 610.64

Feed 2

110–120

481.31

428.24

664.33

Feed 3

86.19–96.19

507.34

395.66

696.45

TABLE 11.1 Pinch Analysis Results for Operating Points of the Three Preheating Phases

Industrial Applications and Case Studies CP [kW/°C] CPH11 = 17.68 CPH12 = 17.68 0.38 1.66 0.84 0.98 CPC11 = 2.92 CPC12 = 5.40 CPC13 = 4.23

CPH11

CPH12

28°

65.5°

C2 101.9 kW 70.0° 40.0° C3 11.3 kW 60.0° 25.4 kW C4

C1

94.2° 507.5 kW 111.3°

1

75.3°

186.0°

2

H1 H2 H3

197.0° 129.8° 40.0° H4 3 C5 75.8 kW 296.3° 140.3° 100.0° 4 H5 C6 39.7 kW 119.8° 130.3° 310.0° 60.0° 65.3° 158.7° 20.0° 1 2 C1 4 H2 3 H1 CPC1 CPC1 CPC11 1 2 56.7 kW 153.5 kW 101.7 kW 11.9 kW 183.6 kW 677.3 kW 3 (a) Initial HEN Feed 1

CPH11 = 9.286 CPH12 = 2.086 0.28 1.25 0.87 1.47 CPC11 = 2.87 CPC12 = 4.25 CPC13 = 4.49

101.7°

28.0° 54.7° C2 C1 436.7 kW 55.7 kW 40.0° 70.0° 1 C3 8.6 kW 60.0° 74.2° C4 17.70 kW 122.1° 40.0° C5 21.4 kW 100.0° C6 137.3° 54.8 kW C1

20.0°

H1

H1 111.6° 186.3°

2 3

294.6°

4

60.0°

64.2°

1

2

112.1°

11.9 kW 140.4 kW

114.8 kW

196.7°

127.3°

3

64.7 kW

180.5°

4

H2 H3 H4 H5

310.0°

H2

231.1 kW 582.8 kW

(b) Initial HEN Feed 2 CPH11 = 9.85 CPH12 = 2.27 0.27 1.15 0.88 1.41 CPC11 = 3.43 CPC12 = 4.25 CPC13 = 4.46

28.0° 48.5° C2 46.6 kW 40.0° C3 8.0 kW

70.0°

C1

96.2° 111.2°

1

60.0° 73.2° C4 15.1 kW 109.4° 40.0° C5 61.2 kW 127.6° 100.0° C6 38.7 kW C1

20.0°

H1

60.0°

137.0 kW

H1

469.9 kW

186.0°

2

197.1°

3

294.8°

4 1

63.2°

2

99.4°

3

117.6°

10.9 kW 129.2 kW 77.7 kW

4

172.2°

235.1 kW

H2

H2 H3 H4 H5

310.0°

614.1 kW

(c) Initial HEN Feed 3

FIGURE 11.4

Initial HEN for the crude-oil preheating process.

matches is needed. This requirement suggests the repiping of coolers mentioned previously, which would form three loops for internal heat transfer. Another important observation concerns the amount of recovery from streams H2 to H5. Streams H3 and H4 feature close supply temperatures. For all three operating points, and especially for that of feed 1, H3 has substantially greater heat capacity flow rate than

259

260

Chapter Eleven H4, which results in a relatively slower decrease in its temperature. This fact and the heat exchanger cascade already planned suggest another topology modification: resequence matches 2 and 3 on stream C1. Such resequencing would yield a larger driving force in both matches, although some load would then be shifted to the lower temperature segment of stream C1. The network was modified according to the strategy and changes suggested by the analysis. The result is shown in Figure 11.5. Cooler C3, on the hot stream with the lowest target temperature, is left at its old location. This, together with the introduced three loops, will account for variations in composition of the feedstock. When there is a larger total heat supply from streams H2 to H5, any heat surplus is removed from the system through cooler C3. Comparing the initial and new topologies reveals that a significant improvement in energy efficiency has been achieved. The heat recovery fraction is increased from 67.03 to 91.22 percent for feed 1, from 73.37 to 89.77 percent for feed 2, and from 74.12 to 77.86 percent for feed 3. Although the relative increase for feed 3 is lower, its net increase in heat recovery is the same as that of feed 2. Based on the simulations for the initial and modified networks, the heat transfer area for each match is determined as recorded in Table 11.2 (where H1 is 4 × 6.26 m 2). The area requirement of the recovery matches EC4 (new), 3, EC5, and EC6 increase after the topology change. Note that only the increase of EC4 is significant, which is due to the heat load shifted from match 2. Another effect of the modification is that the four eliminated steam heating

Feed 1 Match

Initial

Feed 2

Retrofit

Initial

Feed 3

Retrofit

Initial

Retrofit

C1

67.69

67.69

61.62

61.62

75.56

75.56

C2

43.42

43.42

30.51

30.51

31.30

31.30

1

10.83

4.74

8.12

3.44

7.39

4.80

3.45

2.00

2.62

1.61

2.42

0.00

98.04

38.43

69.49

27.21

57.75

31.57

C3 2 C4→EC4 3 C5→EC5 4 C6→EC6 H1 TABLE 11.2

4.95

59.41

3.49

39.97

3.02

12.99

10.67

11.83

11.85

12.30

12.97

15.64

7.99

11.43

2.37

11.17

7.47

5.64

14.58

14.44

24.98

23.84

24.20

24.42

1.81

9.68

2.54

12.01

1.89

2.48

21.33

—

20.98

—

25.04

—

Changes in Heat Transfer Area Due to Retrofit, in [m2]

Industrial Applications and Case Studies 28.0°

65.5°

101.85 kW

C2

52.1°

40.0°

507.47 kW

4.54 kW

130.2°

EC4

40.0°

EC5

27.7°

20.0°

C1

EC5

1

3

H4

63.5 kW

22.3 kW

89.4°

296.3°

147.3°

EC6

137.0°

68.9 kW

H5 165.0°

4

2

3

116.6 kW 46.6 kW

4

120.0°

105.3°

EC4

H3 197.0°

EC6 49.4°

H2

186.0°

2

115.3°

100.0°

H1

111.3°

1

C3

60.0°

94.2°

C1

310.0° H2

92.5 kW 146.6 kW

609.9 kW

(a) Modified HEN Feed 1

28.0°

54.7°

55.7 kW

C2

53.2°

40.0°

436.7 kW

111.6°

1

C3 3.79 kW

60.0°

111.7°

C1

EC4

40.0°

134.5°

117.0°

EC5

100.0°

149.8°

16.7 kW

3

EC6

EC4

66.7 kW 93.3 kW

73.2 kW

4

124.0°

107.0°

81.6°

EC5

1

C1

196.7°

3

EC6 49.1°

25.8°

20.0°

186.3°

2

187.0°

138.0° 2

69.0 kW

294.6°

H2

H3 H4 H5 310.0°

H2

4

64.8 kW

H1

212.7 kW 549.2 kW

(b) Modified HEN Feed 2

28.0°

96.2°

C1 436.72 kW

39.8°

40.0° C3 60.0°

48.5°

55.70 kW

C2

111.2°

1

0 kW

99.4° 2

H3 197.1°

65.1°

EC5

3

H4 122.7°

100.0°

EC6

C1

31.9°

25.5°

20.0° 1 18.9 kW

EC5 22.1 kW

EC4

4 89.4°

54.5°

45.2°

45.1 kW

H2

186.0°

EC4

40.0°

H1

EC6 32.0 kW

3

112.7° 2

116.5 kW 99.1 kW

294.8° H5 169.1°

4 241.9 kW

310.0° H2 608.1 kW

(c) Modified HEN Feed 3

FIGURE 11.5

Modified HEN for the crude-oil preheating process.

exchangers can be used to satisfy the increased area needs for matches 3, EC5, and EC6. Thus the investment, which is estimated to be $42,330, is only for the additional area of EC4. Overall, the modified heat recovery system yields a significant reduction in energy cost. The total sum of savings after the retrofit is estimated

261

262

Chapter Eleven to be $17,519 per year, which results in a reasonable payback period of about 2.4 years (or less if energy prices increase). This case study of a combined problem in heat recovery and process flexibility within a distillation unit’s preheating system combined advanced Pinch-based retrofit methodologies with additional heuristic rules. The result was that the flexibility goals were better met by the introduction of loops in the network topology. In short, the new and modified paths enabled a significant improvement in heat recovery. Another benefit was that the more expensive steam heating was partially replaced by slightly increased furnace duty in the case of higher heat demand. This interesting trade-off between two hot utilities yields an economic benefit owing to the lower cost of furnace fuel.

11.3 Minimizing Water and Wastewater in a Citrus Juice Plant This case study describes a water and wastewater minimization project designed for a citrus plant located in Argentina (Thevendiraraj et al., 2003); the study proceeded by applying the Water Pinch technology (Wang and Smith, 1994). Citrus juice–processing plants consume large quantities of freshwater. The principal objective of this study was to reduce both the freshwater consumed and the wastewater produced by the plant. The citrus processing plant housed the following processes: selection and cleaning, juice extraction, juice treatment, emulsion treatment, and peel treatment. Water minimization was achieved by maximizing water reuse and identifying regeneration opportunities. Water-using operations were represented by the maximum inlet and outlet contaminant concentrations, which are functions of equipment corrosion, fouling limitations, minimum mass transfer driving forces, and limiting water flow rate through an operation. Targets determined the minimum freshwater requirement using the Limiting Composite Curve for the water design network. The graphical Pinch methods that are based on single contaminants can be extended to cover multiple contaminants. When dealing with a number of operations, multiple contaminants, and multiple water sources, the problem becomes more complex and so algorithms using the basic Pinch principles have been developed for solving by MPR-based methods (see Smith, 2005). The study began with data extraction: each stream had to be characterized by its contaminant concentration, inlet and outlet concentration levels, and limiting flow rate through each operation. The data were provided in a schematic flow diagram of the citrus plant that incorporated a simplified water distribution network and the mass balance of the plant’s water streams. Eleven freshwaterusing operations were identified. Chemical oxygen demand (COD)

Industrial Applications and Case Studies was chosen as a component to proxy for all contaminants for two reasons: first, COD measures the most significant contaminant load in the majority of water streams; and second, COD exhibits significantly high values. The overall mass balance is closed by using the assumption that evaporation losses from the steam system amount to 1 t/h (otherwise, there is an “inconsistency” of 1 t/h of water that must be accounted for). The extracted data on contaminant concentrations and water flow rate made it possible to establish the amount of water gained or lost by each operation in the process. The total mass load picked up by the freshwater through each operation was then calculated. The eleven water-using operations—together with the water flow rates entering and leaving each operation—can be represented in the form of a simplified water network, as shown in Figure 11.6. The freshwater COD concentration level for the plant is 30 ppm. There was an existing water reuse between processes currently in the plant, and these reuse streams were left unchanged. The simplified water network presented in Figure 11.6 shows the freshwater-using operations with existing water reuse streams “built in” to each identified operation. The current total freshwater consumed and wastewater generated by this citrus plant were, respectively, 240.3 and 246.1 t/h. The existing water network provided a base starting point for the Water Pinch Analysis. The freshwater target was evaluated by using the Composite Curves. The maximum concentration levels were based on the constraints and limitations dictated by process conditions and requirements. This data were represented in the WATER software tool (2005) with identified constraints. The process restrictions on water type permissible for each operation indicated that operations 2, 4, 5, and 10 can use only freshwater as input. Hence, the minimum freshwater required by plant operations was 164.4 t/h. Operation 1 is a batch process for which the analysis assumed freshwater must always be available. This increases the plant’s total minimum freshwater requirement [t/h] to 164.9 = 164.4 + 0.5 for operation 1. The current total freshwater feed to the plant is 240.3 t/h. These figures can be used to calculate the maximum theoretical freshwater reduction (MTFWR) that is achievable: MTFWR

240.3  164.9 ˜ 100 240.3

31.4 percent

(11.2)

The Water Pinch Analysis was then carried out for the existing water network with maximum concentration levels. The overall freshwater target was calculated using the maximum reuse analysis. Figure 11.7 shows the modified water network represented as a conventional diagram, and the Limiting Composite Curve is plotted

263

264

Chapter Eleven 0.5 t/h

0.5 t/h Packing (1) 1 t/h

Loss to Process 6.265 t/h 7.265 t/h

Loss to Environment 0 t/h

Treatment Plant (Potable) (2)

Boiler

1.000 t/h 26.15 t/h

Blowdown+ Condensate Lossess Neglected 26.15 t/h

Selection / Cleaning (3)

28.093 t/h Gain from Process

Overflow as WW 47.558 t/h 137.558 t/h

APV Condenser & Green Tank (4)

Screen 2&3 & Vincent Press

118.093 t/h

90.0 t/h 240.318 t/h

3.385 t/h

3.385 t/h

246.054 t/h

Vacuum Pump (5) Fresh Water to Plant

1.62 t/h

Screen Taca-Taca (6) Loss to Process

Waste Water from plant

1.62 t/h

4.8 t/h

4.8 t/h Finisher (7) Condensate from distiller stream

1.5 t/h 7.322 t/h Gain from Process Distiller (8) Loss to Process 10.95 t/h 39.6 t/h Screen 1 (9) Loss to Process 15.84 t/h

Condensate from juice vapour 8.822 t/h

28.65 t/h

8.64 t/h Distiller Condenser & Washing Spiral 1 (10) 0.476 t/h

3.6 t/h

7.2 t/h

Gain from Process 4.076 t/h

Centrifugal (11) Total Raw Water Total Waste Water Difference

240.318 t/h 246.054 t/h 5.736 t/h

Total Gain from Process Total Losses to Process Difference

37.391 t/h 31.655 t/h 5.736 t/h

Error % 0.00

FIGURE 11.6

Existing water network (simplified).

in Figure 11.8. The freshwater target was compared with the current freshwater consumption in order to assess the plant’s overall potential for minimizing water and wastewater. The redesigned network yielded a freshwater demand of 169.3 t/h and a wastewater flow rate of 175.1 t/h. Although this amounts to a substantial reduction in both water and wastewater, the design includes reuse of certain streams that will require treatment. As already described, the analysis was based on COD as the pseudocontaminant in reuse streams. However, these streams may well contain other contaminants (e.g., solid waste,

Industrial Applications and Case Studies 0.5 t/h

0.5 t/h

Operation 1

8.96 t/h Loss to Process, 6.265 t/h Recycle, 23.7 t/h 6.265 t/h

2.45 t/h

Operation 2

Loss to Process, 4.8 t/h 4.8 t/h

47.56 t/h Freshwater 169.3 t/h

Operation 3

2.45 t/h

Recycle, 0.83 t/h 0.79 t/h

0.79 t/h Operation 6

Operation 7

Gain from Process, 0.48 t/h 4.01 t/h Operation 11 3.53 t/h Loss to Process, 10.95 t/h 31.83 t/h 39.60 t/h 28.60 t/h Operation 9

Operation 4

Gain from Process, 28.09 t/h 90.00 t/h

Wastewater 175.05 t/h

4.38 t/h 113.72 t/h

Operation 4a

3.39 t/h

3.39 t/h Operation 5 Net gain from Process, 28.09 t/h 8.82 t/h

1.00 t/h Operation 2a/8 Loss to Process 8.64 t/h 15.84 t/h

FIGURE 11.7

Operation 10

7.20 t/h

Water Network after Pinch Analysis as a conventional diagram.

small amounts of chemicals) that require further treatment prior to being used for other processes. Hence additional design options must be developed for dealing with specific process requirements, operating conditions, and suitability standards for water reuse. The necessary design refinements may be achieved by introducing further constraints to potential reuse streams and by utilizing the maximum water reuse analysis to obtain optimal designs that use even less freshwater while meeting all process operating conditions and restrictions. The regeneration reuse analysis can also be used to explore additional design options incorporating the reuse of regenerated water in some operations. Such analysis is based on installation of a treatment unit to regenerate wastewater (by gravity settling, filtration, membranes, activated carbon, biological agents, etc.). This modification would further reduce plant levels of freshwater and wastewater, and it was also evaluated with the WATER software.

265

Chapter Eleven Analysis = Single Component Reference Contm No. 1 [COD] Limiting Composite Curves 30.0 25.0 Concentration [ppb]

266

20.0 15.0 10.0 5.0

0.0

0.2

0.4

0.6

0.8

Mass [t/h] Limiting CC

FIGURE 11.8

Water Supply Line

Limiting Composite Curve generated by WATER software.

Four different design options were generated that considered both the maximum reuse analysis and regeneration reuse analysis (Figure 11.9). Design options A and B were based on the maximum reuse analysis, and both achieve a freshwater consumption of 188 t/h; this is a reduction of about 22 percent from the actual freshwater consumption of 240 t/h. Because of process limitations and restrictions, there was no further scope for water reuse. Yet results from the diagnostic stage indicated that a 31 percent reduction in freshwater and wastewater was possible. This additional extent is achievable by regenerating wastewater and then reusing it in other operations. Design options C and D are based on the regeneration reuse analysis; both result in total freshwater consumption of 169 t/h, which amounts to a 30 percent reduction—that is, nearly all of the theoretical maximum predicted by Eq. (11.2), the expression for MTFWR. The reduction in freshwater use was achieved by rerouting water streams, a modification that requires new pipes. Design option A requires five new pipes; this is fewer than options B or D, which require seven pipes, and option C, which requires nine new pipes. New piping will affect investment cost. The five new pipes identified for design option A are also required in the other options for the same function and at similar flow rates. Therefore, this option requires the least investment and option C the most. Furthermore, design options C and D each require additional investment cost for a

Industrial Applications and Case Studies regeneration unit that is not part of options A and B. These results are summarized in Figure 11.9. Design options A and D are the most attractive ones in terms of maximizing both reuse and regeneration reuse. Option A results in a smaller reduction in freshwater use but at a lower investment cost than option D, which results in a larger reduction in freshwater use but at a much higher investment cost. Wastewater reductions are proportional to freshwater reductions, with corresponding reductions in wastewater treatment costs for each of the options. The cost analysis carried out for design option A indicates attractive financial returns for this low-investment option, whose payback period is only 0.14 years. The outlet water quality of operation 3 required further analysis, so a complete cost evaluation of design option D was not possible. Fully evaluating this option would require additional detailed studies to identify the regeneration process type required and its associated costs. The heat energy of the reuse water streams proposed in the design options was reviewed to ensure that stream temperatures at the inlet of operations remained unchanged. Citrus plant managers reported that nearly all of the process operations occur at ambient temperatures; the only exception was operation 8, which produces wastewater at 90°C. (This particular waste stream is highly contaminated, which imposes some limitations.) All the water reuse streams proposed by the four design options are at appropriate temperatures, so they should not have a thermal effect on operations. The overall hot and cold utility requirements of the plant would not be affected by the changes proposed in the design options. With its existing water network, the plant consumes 240.3 t/h of freshwater and generates 246.1 t/h of wastewater. The proposed design options offer a 30 percent and a 22 percent reduction in freshwater consumption and wastewater generation. For a practical project, the number of modifications is limited. The maximum water

Number of New Pipes Required

FRESHWATER SAVINGS Theoretical Freshwater Reduction Limit, 31% 30

10 5

22

22

5

7

A

B

9

C

Design Options

FIGURE 11.9

Summary of four design options.

30

7 D

% Feed Water Reduction 30 25 20

267

268

Chapter Eleven reuse design requires a minimum of five new pipes, and the regeneration reuse design requires seven new pipes. The reuse analysis predicted a short payback period, but the regeneration analysis was not definitive for the reasons described previously. In sum, a Water Pinch Analysis for this citrus plant demonstrated that the consumption of freshwater could be reduced by as much as 30 percent with low investment and few changes to the existing plant.

11.4 Efficient Energy Use in Other Food and Drink Industries Many studies have employed Pinch Technology (and its associated Heat Integration Analysis) in the food-processing industry. This industry has a far different thermodynamic profile than that of the refining and petrochemical industries. The food-processing industry is characterized by process streams of relatively low temperature (normally 120–140°C), a small number of hot streams, low boilingpoint evaporation of food solutions, considerable deposition of scale in evaporators and heat recovery systems, and seasonal operation. However, a number of studies have also found that the application of Pinch Technology and Heat Integration is hampered by particular aspects of the food-processing systems. These aspects include direct steam heating, difficulties in cleaning heat exchanger surfaces, and high utility temperatures. Despite these drawbacks, the benefits that can be obtained by applying the Pinch Technology (e.g., optimized heat recovery systems and reduced energy consumption) far outweigh the difficulties of performing the studies. There are also other advantages that can be realized by technological improvements: reduced deposition of scale due to reduced utility temperatures, selfregulation of heat processes, and reduced emissions. A case study of the production of refined sunflower oil (Klemeš, Kimenov, and Nenov, 1998) exemplifies the benefits of process analysis based on Pinch Technology and Heat Integration. The process studied operated with a minimal temperature difference of 65°C at the Process Pinch. The external heating required by the system was provided by two types of hot utilities—Dowtherm steam and water steam; the required external cooling was provided by two cold utilities—cooling water and chilled water. The analysis proposed that heat recovery be increased and that the minimum temperature difference be reduced to 8–14°C. The increase in heat recovery (provided by a reduction in the minimum driving force for the process) entailed an increase in the heat transfer area, but this was more than offset by reductions in the hot and cold utility requirements. A further benefit of the analysis was a reduction in the number of utilities needed: eliminating water steam and cooling water considerably simplified the overall design.

Industrial Applications and Case Studies A case study of a whisky distillery by Smith and Linnhoff (1988; see also Caddet, 1994) provides another example of how Pinch Technology and Heat Integration can reduce energy use and increase energy efficiency. In this case it was found that steam was being used below the Process Pinch, resulting in an overall increase in utility usage. The steam was related to use of a heat pump, so the steam used below the Process Pinch was eliminated by reducing the size of that heat pump. Although the steam now had to be used for process heating above the Process Pinch, the overall energy costs were reduced owing to the reduction in compressor duty. Another study involving a whisky distillery was made by Kemp (2007). The hot utility requirement for the process examined was 8 MW, and the Process Pinch was at 95°C. The main hot utility requirements were steam for the distillation system and hot air for the drying system. Kemp showed that the form of the Grand Composite Curve and the temperature of the Pinch could be exploited for heat pumping, and he also suggested that the process would benefit from the introduction of a Combined Heat and Power (CHP) scheme for improved Process Integration and energy efficiency. The site’s power demand was 12 MW, so there were two possibilities for providing both the power and the heat demands from the same utility system. First, a gas turbine that produced 12 MW of power would also supply about 30 MW of high-grade heat from the exhaust. The second option involved the use of backpressure steam turbines, but these would produce nearly 100 MW, much more than what was required. Another advantage of a gas turbine was that its exhaust could be used for drying purposes. Figure 11.10 shows the final configuration of the utility system matched to the GCC. Most of the necessary heat was provided by the gas turbine exhaust and the existing thermo compressors. The existing package boilers were used to provide steam for the thermo compressors. The efficiency of this part of the system was increased by using waste heat from below the Pinch to preheat the boiler feed water. Waste heat boilers driven by the exhaust from the gas turbine provided additional steam. Many processes in the food and drink industry make use of chilling and refrigeration systems. Pinch Technology and Heat Integration have also been used to increase the efficiency of these systems. For example, Fritzson and Berntsson (2006) studied a Swedish slaughtering and meat-processing plant. Their analysis of the plant’s subambient temperature section employed the method proposed by Linnhoff and Dhole (1992) for low-temperature process changes that involve shaftwork targeting. Figure 11.11 shows the plant’s Exergy Grand Composite Curve (EGCC). There is a large gap between the EGCC and the utility curve, which indicates low efficiency in the use of available shaftwork. Improvements in this area could result in a 15 percent reduction in energy demand.

269

Chapter Eleven

xh au st tur

bin

ee

400

300

Ga s

Shifted temperature [°C]

500

200

Waste heat boiler

Site steam Driver steam tu Ga ex rbi s ha ne us t

270

−10

Boiler Feed Water heating Heat pump 0

Cooling water

10

20

30

40

50

60

Net heat flow [MW]

FIGURE 11.10 Final configuration of proposed utility system matched to the process GCC (after Kemp, 2007). 0

500

1000

1500

2000

2500

3000

3500

4000 Q [kW]

0 −0.05

EGCC Utility curve

−0.10 −0.15 −0.20 −0.25 ηc [1]

FIGURE 11.11 Exergy Grand Composite Curve for meat-processing plant (after Fritzson and Berntsson, 2006).

Fritzson and Berntsson (2006) started the energy reduction process by adjusting the loads on the subambient utilities, first maximizing the load on the highest-temperature (−10°C) subambient utility. After this, the load on each lower-temperature utility was

Industrial Applications and Case Studies maximized. The reduction process began at the highest level (the highest temperature), since this utility requirement can be satisfied at a lower cost than refrigeration at lower temperatures. The modified system was then modeled and simulated in HYSYS, which showed a 5 percent reduction in the shaftwork required. However, these results still made for a relatively poor fit between the EGCC and the utility curve. To reduce the gap further, it was suggested that the level of the highest-temperature refrigeration utility be increased from −10°C to −3°C and then the loads be readjusted as before; the result is shown in Figure 11.12. This modified configuration yielded a 10 percent reduction in the shaftwork requirement. Other temperature changes were suggested to reduce further the shaftwork requirements, but these changes were found to be less cost-effective.

11.5 Synthesis of Industrial Utility Systems Varbanov and colleagues (2005) demonstrated the synthesis of a utility system (CHP network) of an industrial Total Site by applying a combination of targeting and Mathematical Programming techniques. Figure 11.13 shows the heating and cooling demands of the chemical site studied. There are two operating scenarios—for winter and summer, with different prices for power and fuel. The basic data for the problem are listed in Tables 11.3 and 11.4. Generic estimates of the corresponding coefficients were specified for the boiler performance (field-erected boilers are slightly more efficient than packaged units), and the capital cost estimates were obtained online (Boiler Cost 2003). These estimates are a function of boiler capacity and steam pressure. The performance and cost of gas

0

500

1000 1500 2000 2500 3000 3500 4000 Q [kW]

0 −0.05

EGCC Utility curve

−0.10 −0.15 −0.20 −0.25 ηc [1]

FIGURE 11.12 Area between the EGCC and the utility curve is further decreased by changing the temperature of the first refrigeration level from −10°C to −3°C (after Fritzson and Berntsson, 2006).

271

272

Chapter Eleven Winter

Summer

T [°C]

T [°C]

300 209.15

209.15 200

−20

130.51

40

20

60

80

−60

−40

198.89 130.51

100

−20

270.68

209.15

200

130.51 LP level candidates

0

HP level candidates

270.68

198.89

130.51 100

−40

300

HP level candidates

0

LP level candidates

20

40

60

80

ΔH [MW]

ΔH [MW]

FIGURE 11.13 Total Site Profiles and candidate steam pressure levels for three steam mains of an industrial chemical site (the Heat Source Profile for summer provides more heat than that for winter).

Winter

Summer

Fraction of year

0.55

0.45

Price of cooling water [$/t]

0.0185

0.0212

Site power demand [MW]

25

31

Maximum export allowed [MW]

10

10

Price of power (import and export) [$/MWh]

20

30

TABLE 11.3

Operating Scenarios for the Total Site

Working hours per year

8600

Interest rate [%]

8

Life of plant [y]

10

Capital installation factor

4.8

ΔTCW [°C]

10

TBFW [°C]

120

P VHP [bar(a)]

90

ΔTVHP,SH [°C]

200

TVP [°C]

50

Natural gas price [$/MWh]

9.369

Distillate oil price [$/MWh]

10.734

Fuel gas price [$/MWh]

4.984

Fuel oil price [$/MWh]

6.226

TABLE 11.4 Site

Configuration Data for the Total

Industrial Applications and Case Studies turbines (ranging from 11.7 to 85.4 MW) were estimated using data from Gas Turbine World (2001). The preliminary Total Site targets estimated minimum utility demand of about 80 t/h for the winter scenario, leading to the choice of a field-erected boiler for stand-alone steam generation. A gas turbine with a Heat Recovery Steam Generator (HRSG) is also selected. For this case, three steam mains (headers) were considered: one for very-high-pressure (VHP) steam generated by the boiler and by the HRSG, and two more intermediate steam mains. The VHP header properties were specified by the problem definition and are given in Table 11.4. Hence, locations for the two other headers still have to be determined. Figure 11.13 illustrates the partitioning of the candidate steam levels, whose ranges are highlighted. For the upper steam main, this graph was used to identify three candidate levels with respective saturation temperatures of 270.68°C, 209.15°C, and 198.89°C; the only candidate for the lower steam main there has a saturation temperature of 130.51°C. The problem superstructure is illustrated in Figure 11.14. Optimizing and reducing the superstructure yields the flowsheet shown in Figure 11.15. It features two fired steam boilers and one steam turbine sized to the steam flow for the winter period. This flowsheet features relatively low on-site power generation and a significant amount of power import. The main reasons behind this approach are that power is cheap and capital is expensive; these factors preclude a better utilization of the steam system’s potential cogeneration. This design also involves a significant amount of CO2 emissions.

Gas turbines gt01

gt01 Process heating demands

Process cooling demands Winter

HRSG

b01

HRSG

b02

VHP: 90 bara, 503.35 °C 12.000 16.885 MW MW 7.700 MW

13.383 MW

1.300 MW

2.877 MW

hdr01: st01

hdr01: st02

hdr01

Canditate pressure levels

tb03 hdr02: st01

15.500 18.136 MW MW

hdr02: st02

hdr02 : tb01

10.632 MW

CT: st01

CT: st02

COND: 0.1235 bara To cooling water

DA

Make-up water

To the stream generators

FIGURE 11.14

3.550 MW

3.175 MW

9.038 MW

5.956 MW

1.635 MW

1.501 MW

50.591 MW

43.777 MW

14.660 MW

10.632 MW

tb01 tb02

8.210 MW

Winter Summer

Summer

Superstructure of the industrial utility system.

Condensate return

273

274

Chapter Eleven Next, potential design measures for reducing greenhouse gas emissions were evaluated. The sensitivity analysis addressed four cases, as summarized in Table 11.5. Case 1 is the base case and thus represents the conditions discussed so far. The other cases gradually increase the price of power and fuel as well as the penalties on emissions. The optimal utility system flowsheet for case 3 is shown in Figure 11.16. Case 4 also replaces fuel oil with a biofuel, which is assumed to have zero CO2 emissions. Analysis of these emission reduction options leads to the following conclusions: (1) Increasing the system efficiency is the cheapest option for CO2 abatement, but it has a relatively limited scope. (2) The next economic option for this particular problem is to close the carbon cycle by using biofuels; in general, however, CO2 capture and sequestration could also be considered.

Winter

b01

Summer

Uses fuel gas Capacity: 51.334 t/h Winter: 51.334 t/h Summer: 45.049 t/h

b02

Uses fuel gas Capacity: 70.000 t/h Winter: 41.990 t/h Summer: 0 t/h

12.000 MW 16.885 MW

Winter

Summer

6.289 t/h

5.625 t/h

VHP: 90 bara, 503.35 °C

3.550 MW 3.175 MW

POWER 7.700 MW 13.383 MW Capacity: 52.409 t/h hdr : st 01 01 Winter: 4.767 MW Winter: 52.409 t/h Summer: 1.941 MW Summer: 26.213 t/h Winter: 15.717 t/h 1.300 MW 2.877 MW Summer: 0.001 t/h 33.139 t/h 25.240 t/h

(tb03)

1.635 MW 1.501 MW 84.620 t/h

23.116 t/h

Winter: 18.769 t/h Summer: 12.493 t/h Winter: 114.025 t/h Summer: 101.182 t/h

To cooling water

To the stream generators

FIGURE 11.15

Case

Condensate return from processes

Winter: 136.671 t/h Winter: 22.646 t/h Summer: 116.369 t/h Summer: 15.187 t/h Make-up water

Winter: 154.502 t/h Summer: 128.237 t/h

17.597 t/h

14.660 MW 10.632 MW

COND: 0.1235 bara DA

77.960 t/h

50.591 MW 43.777 MW

TSAT=130.51 °C (tb01); P=2.74 bara

8.210 MW 10.632 MW

5.956 MW

Winter: 16.645 t/h Summer: 0.558 t/h

29.533 t/h

15.500 MW 18.136 MW

13.210 t/h

9.038 MW

P=15.19 bara

TSAT=198.89 °C;

52.304 t/h

18.907 t/h

Power import [MW]: 21.1 (Winter); 30.0 (Summer) Total annualized cost: 13.124 · 106 $/y

Optimal utility system for Case 1 (base case).

Price of CO2 [$/t]

Price of SOx [$/t]

Price of NOx [$/t]

Power price [$/MWh]

1

0

0

0

20.00

30.00

2

0

0

0

30.00

45.00

3

40

500

1000

40.00

60.00

4

40

500

1000

40.00

60.00

TABLE 11.5

Parameters

Sensitivity Analysis for Reducing Emissions: Basic

Industrial Applications and Case Studies Power Capacity: 33.917 MW Winter: 30.085 MW Summer: 33.916 MW

gt01

Winter

Summer

Capacity: 28.570 t/h Winter: 0.000 t/h Summer: 0.000 t/h

Winter: 95.230 t/h Summer: 45.022 t/h

Winter

b02

HRSG 12.000 MW 16.885 MW VHP: 90 bara, 503.35°C 7.700 MW

1.300 MW

Power Capacity: 52.017 t/h hdr01 : st01 Winter: 7.722 MW Winter: 52.017 t/h Summer: 1.942 MW Summer: 26.023 t/h

13.383 MW

2.877 MW TSAT = 198.89°C;

33.139 t/h 25.240 t/h

(tb03)

Power Capacity: 20.000 t/h hdr02 : st01 Winter: 0.733 MW Winter: 13.997 t/h Summer: 0.000 MW Summer: 0.000 t/h

29.533 t/h

TSAT = 130.51°C; 10.632 MW

P=2.74 bara

Winter: 19.869 t/h Summer: 12.491 t/h

To cooling water DA

(tb01)

5.625 t/h

3.550 MW

3.175 MW

18.907 t/h

13.210 t/h

9.038 MW

5.956 MW

1.635 MW

1.501 MW

Winter: 18.016 t/h Summer: 0.164 t/h

52.304 t/h

15.500 MW 18.136 MW

8.210 MW

P=15.19 bara

Summer

6.289 t/h

Winter: 4.904 t/h Summer: 0.555 t/h

84.271 t/h

77.935 t/h

50.591 MW

43.777 MW

24.272 t/h

17.597 t/h

14.660 MW

10.632 MW

COND: 0.1235 bara Winter: 114.832 t/h Condensate return Summer: 101.157 t/h from processes Winter: 22.758 t/h Summer: 15.119 t/h Make-up Power export [MW]: 10.0 (Winter); 4.4 (Summer) water Total annualized cost: 23.060 · 106 $/y

Winter: 137.590 t/h Summer: 116.343 t/h To the stream generators

FIGURE 11.16

11.6

Winter: 156.466 t/h Summer: 128.209 t/h

Optimal utility system for Case 3.

Heat and Power Integration in Buildings and Building Complexes Herrera, Islas, and Arriola (2003) studied a hospital complex that included an institute, a general hospital, a regional laundry center, a sports center, and some other public buildings. The use of diesel fuel represented 75 percent of its total energy consumption and 68 percent of its total energy cost, which was $396,131 in 1999. In the hospital complex, the heat demand is met by producing steam in boilers fueled by high-price diesel fuel. There is no heat recovery between the existing heat sources and heat sinks. The hot streams were identified as the soiled soapy water from the laundry and the flow of condensed steam not recovered in the condensation network. The stream data are presented in Table 11.6. For this hospital complex, the amount of external heating required (i.e., the hot utility target) is 388.64 kW, which can be seen on the hot and cold Composite Curves in Figure 11.17. This plot was employed to determine what temperature levels of the utilities would satisfy this requirement. The heating utility target of 388.64 kW translates to an annual energy requirement of 12.26 TJ/y. The amount of heating provided is actually 625.28 kW, which represents the heat services that are currently transferred to the complex. This figure represents a potential for energy savings of 38 percent, which is equivalent to an annual reduction in diesel fuel of 246,000 liters (worth about $100,000). To reduce heating energy demands to the targeted value, the Heat Integration Analysis

275

276

Chapter Eleven Stream

Name

T supply [°C]

T target [°C]

DH [kW]

CP [kW/°C]

1 Hot

Soapy water

85

40

23.70

0.53

2 Hot

Condensed steam

80

40

96.32

2.41

3 Cold

Laundry sanitary water

25

55

17.60

0.59

4 Cold

Laundry

55

85

77.27

2.58

5 Cold

Boiler feed water

30

60

7.13

0.24

6 Cold

Sanitary water

25

60

77.12

2.20

7 Cold

Sterilization

30

121

12.50

0.14

8 Cold

Swimming pool water

25

28

151.67

50.56

9 Cold

Cooking

30

100

59.63

0.85

10 Cold

Heating

18

25

100.82

14.40

11 Cold

Bedpan washers

21

121

4.94

0.05

TABLE 11.6

Process Stream Data of Hospital Complex (Herrera, Islas, and Arriola, 2003) T [°C] 120

Hot CC Cold CC

100 80 60 40 PINCH 20 0

FIGURE 11.17

80

160

240

320

400

480

ΔH [MW]

Process Composite Curves for hospital complex (∆Tmin = 20°C).

indicates that four extra heat exchangers should be added to the network. Two are needed in the laundry to cover part of the heat demand, a third is needed in the machinery rooms that help to heat boiler feed water, and a fourth is needed in the condensation tank area that heats the sanitary water. The analysis could be refined

Industrial Applications and Case Studies further by considering several other issues, such as fouling, pressure drop, and variation in the heat demand.

11.7 Optimal Design of a Supply Chain In the global market, optimal management control of a company is necessary for survival. Such control involves a series of effective strategic decisions that are concerned with various aspects of the supply chain—for example, decisions regarding the products themselves as well as the location of production facilities and distribution centers. When the subject is the development or operation of highly complex business processes (e.g., supply chains, value chains), computer-aided decisions are preferred. A conventional approach for systematically evaluating decision alternatives is Mathematical Programming, although a daily management problem is usually not resolved via MPR methods. Even when the MPR can be constructed for the problem, it is still difficult to verify whether the mathematical formulation of relevant decision alternatives is sufficiently accurate and complete to identify the optimal solution. When the mathematical model is not generated systematically, the model’s chances of embodying the optimal solution are very low. This case study involves determining the optimal design of a supply chain. Here, the purpose of the supply chain is to meet a given volume demand for commodity C at location L1. Three options are considered: produce commodity C at location L1; produce commodity C at location L2 and then transport it to location L1; or some combination of these. Production requires the availability of part A and part B at the same location. Part A is available at location L3 and, to a limited extent, at location L4; it can be transported to location L1 or to location L2. Part B is available at location L2 and can be transported to location L1. The list of potential activities is given in Table 11.7. ID

Activity

Location

Precondition

Effect

PL1

Production

L1

A and B at L1

C at L1

PL2

Production

L2

A and B at L2

C at L2

TAL3L1

Transportation

From L3 to L1

A at L3

A at L1

TAL3L2

Transportation

From L3 to L2

A at L3

A at L2

TAL4L1

Transportation

From L4 to L1

A at L4

A at L1

TAL4L2

Transportation

From L4 to L2

A at L4

A at L2

TBL2L1

Transportation

From L2 to L1

B at L2

B at L1

TCL2L1

Transportation

From L2 to L1

C at L2

C at L1

TABLE 11.7

Potential Activities in the Supply Chain Case Study

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278

Chapter Eleven Given the list of potential activities defined by their preconditions (activating entities) and effects (resulting entities), the Maximal Structure Generation (MSG) algorithm then produces the maximal structure (Friedler et al., 1993). Next, when applied to the maximal structure so derived, the Solution Structures Generation (SSG) algorithm (Friedler et al., 1995) enumerates 15 combinatorially feasible business process structures for the problem. To determine the optimal business practice, the following quantitative information is provided in addition to the case study’s 15 structural alternatives. The required volume of the demand is 20,000 pieces annually. Producing one piece of commodity C requires the availability of one piece of part A and one of part B. At most 5000 pieces of part A are available at location L4 for €230 each. An unlimited number of part A can be purchased at location L3 for €250 each, and an unlimited number of part B can be purchased at location L2 for €310 each. The cost of an activity depends on its volume. To estimate the increase in the cost of an activity as a function of its volume, costs are given for handling 1000 and 2000 pieces per year. If a linear cost function with a fixed charge is adopted to estimate the cost of the activities with different volumes, then this function is determined by the fixed charge and the proportionality constant. Table 11.8 summarizes the cost of processing 1000 versus 2000 pieces per annum as well as the parameters of the fixed-charge linear cost function for each activity. The optimal business process, as determined by the Accelerated Branch-and-Bound (ABB) algorithm (Friedler et al., 1996), corresponds to the activities given in Table 11.9 whose annual cost totals

Activity ID

Cost of processing

Cost function parameters

1000 pcs/y [€/y]

2000 pcs/y [€/y]

Fixed charge [€/y]

Proportionality constant [€/pcs/y]

PL1

8,000

10,000

6,000

2

PL2

9,000

10,000

8,000

1

TAL3L1

4,000

8,000

0

4

TAL3L2

10,000

20,000

0

10

TAL4L1

12,000

24,000

0

12

TAL4L2

2,000

4,000

0

2

TBL2L1

10,000

20,000

0

10

TCL2L1

14,000

28,000

0

14

TABLE 11.8

Cost of Activities in the Supply Chain Case Study

Industrial Applications and Case Studies Activity ID

Optimal

2nd best

3rd best

Volume [pcs/y] PL1

15,000

PL2

5,000

TAL3L1

15,000

20,000 20,000 15,000

TAL3L2

15,000

TAL4L1

5,000

TAL4L2

5,000

TBL2L1

15,000

TCL2L1

5,000

Total cost [€/y] TABLE 11.9 Processes

11,439,000

5,000 20,000 20,000 11,466,000

11,568,000

Activities in the Optimal, Second-Best, and Third-Best Business

€11,439,000. The second-best business process has a total annual cost of €11,466,000, and the third-best business process has a total annual cost of €11,568,000.

11.8 Scheduling a Large-Scale Paint Production System Paint production usually consists of three major operations: grinding and dispersion, mixing and coloring, and discharging and packaging. Paints and coatings are typically produced in batches. They are made in stationary and portable equipment units such as high-speed dispersion mixers, rotary batch mixers, blenders, sand mills, and tanks. The raw materials are solvents, resins, pigments, and additives that include inorganic and organic chemicals. Paint manufacturing does not usually involve chemical reactions between the raw materials, so the finished product consists of a mixture of the different raw materials. Several dozens of products are produced at the manufacturing site, so the corresponding scheduling problem is bound to be highly complex. The S-graph framework of batch scheduling (see Chapter 7) has been extended to solve complex paint production problems (Adonyi et al., 2008). Changeover time is defined for any equipment unit that requires cleaning. Traditionally, minimizing makespan (total time to completion) is the criterion used when assigning equipment units to tasks and scheduling the tasks. Such schedules maximize the production system’s efficiency, but they may lead to unnecessarily high levels of waste generation. Thus, determining which task schedule minimizes cleaning cost will require that the problem’s objective function be modified. Now, rather than minimizing makespan as in the original problem, the reformulation seeks to

279

280

Chapter Eleven minimize the cleaning cost. This change in criterion has only a minor effect on the solution procedure, so an effective solver for the original problem is also useful for the reformulated problem. Twenty-three equipment units, E1 through E23, are available to generate six products, A through F. The changeover time is 70 minutes for equipment units E6, E7, E8, and E9 but 100 minutes for equipment units E1 through E5 and E10 through E20. All other changeover times are presumed to be zero. The number of batches to be produced is given in Table 11.10. Cleaning the equipment units is a costly operation that involves many pollutants. The minimal makespan schedule contains 11 cleaning operations, which are denoted by the dotted changeover arcs on its S-graph; see Figure 11.18. The cleaning cost of the solution with minimal makespan is $14,000. In contrast, the solution based on minimizing the cost involves four (rather than 11) cleaning operations and only $3,500 in cleaning cost; its makespan is 6,910 minutes. If the cleaning cost is limited to reach $5,500, then the corresponding makespan is reduced to 6,700 minutes. Product

A

B

C

D

E

F

Number of batches

3

5

1

3

9

3

TABLE 11.10

E1

60

E6

60

E11

120

0

0 E1

310

Number of Batches Produced of Each Product

E6

310

E11

120

E11

120

E15

98

E22

540

99

120

E22

540

E6

310

E1

60

E7

240

E1

60

E7

240

E1

60

E19

120

E22

E7

240

E11

100 120 E22 540

E1

60

E1

60

E7

E2

60

E8 120

60

E7

0

0 0

0 E7

102

60

E22

540

240

E15

100 120 E22

540

E16

50

E22

540

E18

90

E22

E14

90

E22

540

107

E20

60

E23

720

108

103

0 104

0

E3

60

240

E7

0

240

540

106

0

0

0 60

0 E7

70 E4

A

B 70

E4

240

70

E4

B

E4

B

D

40

E6

120

E10

60

E6

120

E12

90

0

0 40

E21

E6

E6

120

0

0 E10

60

300

E12

E6

300

0

60

0

40

E6

300

90

0

0 40

E6

300

E6

300

0

60

90

E6

40

E7

300

114

0 720

115

0 E21

0

40

720

E21 0

E12

720 113

E21 0

E10

0

0 40

0 E21

0 E12

720 112

E21 0

E10

720 111

E21

90

0

0 40

109

720 110

E21

0

40

720 0

0 E4

720

116

0 E16

90

E21

720

117

100 E5

D

D

0

0 E4

B

C

40

0 E4

100 105

0

E3

A

540 101 B 0

E13

70

E3

E4

0

240 0

0

100

0

0

0

E4

A

0

70

0

0

E22 0

60

97

0 540

0

0 E1

540

E22 0

100

40 0

E7

0 E5

E19

120

E23

0

0 E5

240

40

E7

240 0 240

E20

60

E23

720 0 720

118

119

0 E15

120

E23

720

120

E

E

E

E

E

E

E

E

E

F

F

F

100

FIGURE 11.18 Schedule graph of the solution that minimizes makespan (after Adonyi et al., 2008).

CHAPTER

12

Typical Pitfalls and How to Avoid Them

P

rocess Integration (PI) has proven to be a powerful optimization tool for designing processes that are energy-efficient, environmentally friendly, and sustainable. The methodology provides clear insight into the design process, but this direct simplicity is sometimes misunderstood by potential users. Once proper data are made available, the procedure generates an excellent lead for the design process. But just as with all optimization tools, potential pitfalls when using PI include improper formulation of the problem and incorrect data extraction. Even when the most efficient and well-developed methodology is used to solve an optimization problem with high precision, the results may be suspicious unless we have been solving the right problem. In other words, has the problem been formulated in a way that closely reflects the real process under consideration and (especially) has the correct data been extracted? Negative answers to these questions explain such published statements as: “Pinch technology [or process integration] did not work for this problem.” When these problems are revisited it usually becomes obvious that the PI methodology is not at fault; rather, an inexperienced or overconfident user is typically the cause. Therefore, this chapter is devoted to various mistakes that a designer might unwittingly make. The most basic issue concerns how one starts a PI-based project and how it is run. Kemp (2007) summarized the key steps listed below, which have been further developed based on the authors’ experience. These steps are specifically related to Heat Integration; however, they apply with only small adjustments to mass, water, and other integration as well. 1. Become familiar with the analyzed process. The most efficient way is to closely liaise with the process designer and/or plant manager, especially if the plant is already operating.

281

282

Chapter Twelve 2. Develop a mass and heat balance. This should be based on the designed process flowsheet data and calculations and/ or on measurements taken from the operating plant (if the study is for a retrofit). 3. Select the streams. This is a critical step and, as will be shown in this chapter, not as straightforward as it may seem. 4. Remove all the existing units related to the PI analysis. For Heat Integration, remove all heat-transferring units, for mass water integration remove all water interconnections (the pipes). This step is also critical—without it, the optimized design would not differ from the initial design. Section 4.2.4 provides an example illustrating this activity. 5. Extract the stream data for the PI analysis. Different data are relevant for each PI analysis type. For HI heat loads and temperatures are extracted. 6. Make a qualified initial guess for the ΔTmin value; this value can be adjusted later at various stages of the design optimization. 7. Perform the Pinch analysis: obtain the Pinch temperatures and the utility targets. 8. Design the initial (heat exchanger) network using the criterion of maximizing energy recovery. 9. Check for a cross-Pinch transfer and for inappropriate placement of utilities. 10. Check for proper placement of reactors, separation columns, heat engines, and heat pumps. 11. Investigate the potential for further modifying the process in order to minimize energy consumption and reduce capital costs. Investigate the potential benefits of applying the plus-minus principle (see Chapter 4) and the KHSH and KCSC principles (see Figure 4.44). 12. Investigate the potential for integration with other processes— that is, Total Site Analysis. 13. Consider the implications of pressure drop (trade-offs between heat savings and extra energy for pumping) and the physical layout (capital cost of heat exchangers and/or piping). 14. Make the preselection of heat exchange equipment and perform the preliminary costing. Provision should be made for variations in the future price of energy. 15. Make the first optimization run of the predesign plant or site, and make adjustments to ΔTmin.

Typical Pit falls and How to Avoid Them 16. Based on the optimization, extract adjusted data and return to step 7. Perform an additional loop (or loops) while screening and scoping for potential simplifications. 17. Consider real plant constraints; these include safety, technology limitations, controllability, operability, flexibility, availability, and maintainability. 18. Pay attention to start-up and shutdown of the process; some early designs for highly integrated plants had problems in this area. 19. Run a second optimization for the final tuning accounting for the information added during steps 16 to 18. If necessary, return to any appropriate previous step for adjustment. 20. The design is now ready for detailing. However, optimization is a never-ending procedure, and designs may need to be modified in response to changes in operating conditions (e.g., plant capacity) or the economic environment (e.g., tax policy; prices for energy, materials, and production).

12.1

Data Extraction As emphasized previously, data extraction is a crucial step. Bodo Linnhoff presented one of his last plenary lectures (Linnhoff and Akinradewo, 1998) on the automated interface between simulation and integration. This has been a substantial step toward data extraction for PI software tools. The plenary has been fairly comprehensive and suggested the way forward for this important task. The problem received increased interest following this lecture, and several software packages now offer support for solving it. Nonetheless, more work in this area is needed to satisfy the requirements of routine industrial applications. In their SuperTarget and Pinch Express software packages, Linnhoff March (1998) included procedures for automatic extraction of data for Heat Integration. Even so, thermal data, which involve the stream heating and cooling information and utilities information, are the most critical data required for Pinch Analysis. There are several possibilities for extracting the thermal data from a given heat and material balance. This must be done carefully, as poor data extraction can easily lead to missed opportunities for improved process design. In extreme cases, poor data extraction can falsely present the existing process flow-sheet as optimal in terms of energy efficiency. If the data extraction accepts all the features of the existing flow-sheet then there will be no scope for improvement. If it does not accept any features of the existing flow-sheet then Pinch Analysis

283

284

Chapter Twelve may over-estimate the potential benefits. Appropriate data extraction accepts only the critical sections of the plant which cannot be changed. Data extraction skill develops with increased experience in the application of Pinch Technology (Linnhoff March, 1998). Since the release of these packages, the methodology has developed further and more attempts have been made to extract data automatically. However, experience and following the proper rules remain valuable assets. Basic questions to ask include the following: 1. When is a stream a stream? 2. How precise must the data be at each step? 3. How can considerable changes in specific heat capacities be handled? 4. What rules and guidelines must be followed to extract data properly? 5. How can the heat loads, heat capacities, and temperatures of an extracted stream be calculated? 6. How “soft” are the data in a plant or process flowsheet? 7. How can capital costs and operating costs be estimated?

12.1.1 When Is a Stream a Stream? To those unfamiliar with PI, identifying a stream seems fairly straightforward. In fact, many considerations are involved, and accounting for them properly is key to setting up the problem. First, we need not consider any stream that neither gains nor provides heat; no data needs to be extracted from a stream with identical supply and target temperatures and enthalpies. (Of course, in the absence of perfect insulation, every stream loses or gains some heat; in many cases, however, these small amounts of losses and gains can be neglected.) If we do not extract data from such streams, the problem is considerably simplified. There are also streams that, for one reason or another, should not be included in the PI problem—for example, streams that are remote and streams that should not be altered for safety, product purity, and operational reasons and for other (mostly practical) considerations. Finally, Heat Integration deals with heat flows, which can be carried not only by a pipe line but also by radiation or conduction. Consider the example depicted in Figure 12.1. This example was introduced, along with some data extraction rules, by Linnhoff and colleagues (1982) and was later modified for use in many follow-up books (e.g., Smith, 1995; Smith, 2005; Kemp, 2007) and in many courses based on UMIST (later the University of Manchester) teaching materials. The figure shows part of a flowsheet in which the feed stream is heated to 45°C by recuperated heat in a heat exchanger and then enters a processing unit. After leaving this unit, the stream is

Typical Pit falls and How to Avoid Them

150° 160° ΔH3 190° 120° Reactor

40°

80°

45°

10°

45°

ΔH2 140°

FIGURE 12.1

ΔH1 Unit

Feed

140°

Partial flowsheet for example process.

heated further by two heat exchangers and then enters a reactor. The reactor requires the feed stream to be at 165°C. The question is: How many streams should be extracted? 1. Three streams: 10–45°C, 45–80°C, and 80–165°C 2. Two streams: 10–45°C and 45–165°C 3. One stream: 10–165°C Choosing option 1 yields a design exactly like the original one; there will again be three heat exchangers with the same heat transfer duties as before. This case accounts for claims of “no process improvement” by some PI critics. Option 2 presents more degrees of freedom: the first heat exchanger would be the same, but the other could be modified. Extracting two streams would be appropriate for cases when the processing unit requires a feed temperature of close to 80°C. Option 3 provides the most degrees of freedom and scope for improvement, but with this design the processing unit feed could be at any temperature between the 10°C supply and the reactor target of 165°C. If the processing unit is, say, a filter (as assumed by Smith, 2005), then there would probably be some restriction on the filter supply temperature to ensure proper operation of the filter. If the processing unit is storage (as assumed by Linnhoff et al., 1982), then the supply temperature might be restricted to a different range (depending, e.g., on whether liquid or gas is stored). This simple example demonstrates that choosing the right stream from which to extract data cannot be a fully automatic process. Making this choice requires assessments related to specific processing units and performance requirements for the plant.

12.1.2

How Precise Must the Data Be at Each Step?

There are frequently questions about required data precision, and a common excuse for not applying PI analysis is that the data on a plant is not sufficiently precise. However, the process of applying PI

285

286

Chapter Twelve is itself based on (initially) rough assumptions, which are revised during the course of several design loops. At the beginning there are no specifications for the heat-transferring units, and neither are the feed temperatures (and several other important factors) fully fixed. At this stage, then, extremely precise data is not needed. It is important to recognize that PI and the initial optimization are more about screening and scoping than about detailed design. In seeking potential energy savings, it is the general direction in which optimization should proceed that is the initial concern. If the result of this first step is that a 15 percent savings in energy is possible, then this figure is sufficient to confirm the design approach and it doesn’t much matter if the precise figure is actually 13 or 17 percent. It is in the regions close to the Pinch that the data should be as precise as possible (Linnhoff et al., 1982). Also, it is best to remain inside the Composite Curves in the plot of temperature versus enthalpy. At the start of data extraction, we might have only a vague idea of where (and at what temperature) the Process Pinch will occur; also, the Composite Curves are based solely on data extraction. Therefore, data extraction must necessarily start from rough assessments and then be corrected step by step.

12.1.3 How Can Considerable Changes in Specific Heat Capacities Be Handled? Further analysis of the flowsheet in Figure 12.1 reveals that phase changes are very likely to occur when the temperature increases from 10°C to 165°C. In general, Cp varies with temperature, but latent heat is also a determining factor. Clearly, using a constant value for Cp would not be sufficiently realistic. A segmentation technique has been developed to deal with this problem. This technique is used, for example, in the software tools SPRINT (2009) and STAR (2009). The software tools treat the segments as individual streams that are combined to form input and output streams. Data extraction is affected by how many segments are used and their boundary temperatures (see Figure 12.2). Increasing the number of segments naturally increases the complexity, so this

T

1

T

?

T

? ΔH

FIGURE 12.2

2

3

T

? ΔH

How should we linearize?

4

? ΔH

ΔH

Typical Pit falls and How to Avoid Them number should be minimized for industrial problems involving many streams.

12.1.4 What Rules and Guidelines Must Be Followed to Extract Data Properly? As mentioned in Section 12.1.1, data extraction rules were first introduced by Linnhoff et al. (1982) and frequently used with some modifications thereafter (Smith, 1995; CPI, 2004 and 2005; Smith, 2005; Kemp, 2007). Most of this work is related to Heat Integration, but the principles apply as well to mass (water) integration. These rules are reviewed briefly in this section. When two or more streams of different temperatures are mixed, this nonisothermal mixing constitutes a heat exchange with degradation of the higher temperature. In some cases, such mixing can also cause cross-Pinch transfer problems—as in Figure 12.3(a),

FIGURE 12.3 Nonisothermal stream mixing extracted as (a) three streams and (b) two streams.

(a)

160°

110° 70°

40°

75°

110°

35°

160°

40°

70°

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(b)

160°

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40°

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35°

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Chapter Twelve where three streams are extracted. The correct data extraction for this case involves two streams, as shown in Figure 12.3(b). General guidelines for data extraction may be summarized as follows: 1. Heat losses. In most cases, heat losses can be neglected. However, they should not be neglected when streams (mass and heat flow in pipes) are long or subject to varied temperatures. In such cases, the solution is to introduce hypothetical coolers (or heaters) that represent the heat loss. 2. Extracting utilities. The utilities should never be extracted from the existing plant or flowsheet, for then the solution would likely arrive at the same utility values and perhaps neglect some options that would be more efficient. This rule of thumb applies especially to cases where utilities can be generated on-site and thereby (at least partially) replace costly existing utilities. In this connection it should be remembered that steam is not always a utility—sometimes it is also a process stream (e.g., stripping steam in separation columns). Process streams should remain in place and not be removed. 3. Generating utilities. The Heat Integration analysis may indicate some valuable options for using otherwise wasted heat or cold to generate utilities. The Grand Composite Curves can be used to locate such options. However, when extracting data it must be recognized that steam requires the boiler feedwater (BFW) to be heated, water to be evaporated, and the steam to be superheated; see Figure 12.4. Many mistakes have been caused by designers who simply matched the T Specified Steam Conditions

BFW Conditions ΔH

FIGURE 12.4 Extraction of a cold stream including segments for BFW preheating, evaporation, and superheating.

Typical Pit falls and How to Avoid Them steam generation line without making provisions for preheating and superheating. 4. Extracting at the effective temperature. In some cases a stream cannot be extracted directly because it has to still be used by a related process. For example, a hot stream should be extracted at temperatures at which the heat becomes available. An example is given in Smith (2005, p. 433) for a reactor using a quench liquid. 5. Forced and prohibited matches. In almost any process there exist matches that are necessary for technological reasons—the forced matches—as well as those, such as hot and cold stream matches in a heat exchanger, that should be prohibited (e.g., to prevent contamination of one of the streams). In manual design these constraints have to be observed by the designer, but software tools usually offer this option. If not then the constraints can be secured by an appropriate penalty or bonus (as applies) in the objective function used for the optimization. 6. Keeping streams separate only when necessary. If streams can be merged then it may be possible to eliminate some heatexchanging units. For example, streams that leave the plant to be treated as wastewater often have some heat content that can be utilized.

12.1.5 How Can the Heat Loads, Heat Capacities, and Temperatures of an Extracted Stream Be Calculated? Once a stream has been extracted, the next problem is calculating the heat-related data. There are standard engineering procedures available for the running plants as the measurements with the following data reconciliation (Klemeš, Luťcha, and Vašek, 1979; Minet et al., 2001; VALI III User Guide, 2003). The other option is to develop a flowsheeting simulation model (Klemeš, 1977). An overview of flowsheeting and balancing simulators was given in Chapter 9. If a plant is being designed, some data could be also extracted from the process flow diagram (PFD). But all those options consume time and resources, so in the early design stages (when the process structure is still under development and likely to be changed as a result of PI analysis), it is reasonable and easier to use a simplified approach based on the extracted data. Such an approach is demonstrated in Figure 12.5 for a part of the flowsheet from Figure 12.1. The CPs of the stream segments are assumed constant and calculated from the temperatures and the duties given in the flowsheet. Experience has indicated that the resulting rough preliminary data are sufficient and can later be made more precise by one or more of the procedures listed previously.

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Chapter Twelve T 160°

80° 45° 150° 160°

10°

ΔH3

ΔH1 ΔH2

ΔH

ΔH3

190° 120° Reactor

40°

80°

45°

45°

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ΔH2 140°

ΔH1 Unit

Feed

140°

FIGURE 12.5 Obtaining rough data from flowsheet heat loads and temperatures.

12.1.6 How “Soft” Are the Data in a Plant or Process Flowsheet? Distinguishing soft data from hard data is one of the most important aspects of data extraction. Inexperienced persons are usually trying to stick the temperatures shown in the PFD, extract those temperatures, and then perform the PI analysis. However, this approach usually ends up overlooking many opportunities. A better approach is to question every temperature, discuss each one with the process engineer (or plant designer or plant manager), and thereby establish which temperatures are critical (the “hard” data) while the rest (the “soft” data) can be in some way compromised. In practice, most data are at least a little soft, and designers can use this fact to their advantage. Typically, streams that are leaving the plant (see Figure 12.6) are characterized by soft data and thus are suitable for optimization via the plus-minus principle (Figure 12.7). Data softness is closely related to changing conditions and to a design’s flexibility, operability, and resilience.

12.1.7 How Can Capital Costs and Operating Costs Be Estimated? The need to find cost data arises when the appropriate ΔTmin (which should be close to the optimum) is being selected. The optimum ΔTmin depends strongly on economic parameters, and its value is important for both grassroots design and retrofit. Estimating capital costs is usually a time-consuming procedure. However, it is possible to use

Typical Pit falls and How to Avoid Them

110°

70°

Storage 70°

110°

Cooler

FIGURE 12.6

20°

Storage 20°

Cooler

Soft data for streams leaving a plant.

T

T Decrease (–) Hot Stream

Reduced Cold Utility Target

Increase (+) Hot Stream

Reduced Hot Utility Target

ΔH T

ΔH T

Increase (+) Cold Stream

Reduced Cold Utility Target ΔH

Decrease (–) Cold Stream

Reduced Hot Utility Target ΔH

FIGURE 12.7 The plus-minus principle can be used to optimize application targets by using properly extracted soft data.

approximate methods (Taal et al., 2003) at the initial design stage, when little is known about the types of heat transfer units to be used, the ultimate design, the materials required, or the temperature, pressure, and composition of streams. The estimates so derived will usually suffice until the final detailed design cost date, at which time information is obtained from selected manufacturers. Note, however, that equipment cost may vary regionally and may also be related to market conditions (e.g., a large customer can secure discounts, and prices fall during a recession). It is much more difficult to establish operating cost, which is affected by labor, taxation, and so forth but is mainly a function of energy cost. Here the most obvious problem—and greatest potential pitfall—is using the current price of energy. (It is possible to find

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Chapter Twelve many publications and projects where this rule was not followed.) It is better to use the anticipated average energy price for the life span of the plant or, in the case of a retrofit, for the payback period. The problem then becomes one of estimating this future energy price for periods that may be as long as five or ten years. It has been shown (see, e.g., Klemeš and Bulatov, 2001; Donnelly, Klemeš, and Perry, 2005) that even the forecasts of highly qualified experts are frequently inaccurate. One of the obvious potential approaches is to use the scenarios and target the most flexible design that would provide a balanced optimum for various situations.

12.2 Integration of Renewables: Fluctuating Demand and Supply The integration of renewable energy sources was discussed in Chapter 6. Renewable resources are usually available on a smaller scale and are often distributed over a certain region. Their availability (with the exception of biomass) varies significantly with time and location. This variability is due to changing weather and geographic conditions. The energy demands (heating, cooling, and power) of sites also vary significantly with time of the day and period of the year. These variations in the supply and demand of renewables can be predicted in part, and some of the variation is fairly regular—for instance, day versus night in predominantly cloudless areas for solar energy. The availability of wind-generated energy can be less predictable. One approach to dealing with these problems is the advanced PI technique that employs time as an additional problem dimension. A basic methodology along these lines (involving “Time Slices” and Time Average Composite Curves) was developed for the Heat Integration of batch processes (Klemeš et al., 1994; Kemp and Deakin, 1998). This methodology was recently revisited by Foo, Chew, and Lee (2008). This methodology has also been extended to the Heat Integration of renewables. Important steps in this direction were reported by Perry, Klemeš, and Bulatov (2008) and Varbanov and Klemeš (2010). Dealing with variation and fluctuation brought another complexity into data extraction. Data should be collected for all time slices that increase the complexity. Especially, for each case, it is necessary to choose the time horizon for the analysis and number of time slices. This is a fast-developing field, so it is advisable to monitor recently published research papers and conference presentations.

12.3 Steady-State and Dynamic Performance It has been assumed that all analyzed and optimized processes operate in a steady state. Many industrial processes do operate in this

Typical Pit falls and How to Avoid Them fashion, and a common control task is to maintain such processes in a steady state. However, there are also many situations in which the working regime must be changed. This occurs not only at start-up and shutdown but also in response to changes in operating conditions (e.g., outside temperatures) and production conditions (e.g., capacity, volume). Problems involving such variation are generally addressed in one of two ways: (1) accommodating various scenarios via a design objective of minimizing sensitivity to the possible changes or (2) designing to optimize the total system’s overall dynamic performance. The second option is much more complicated and requires more time and resources; hence it is used only when substantial deviations from steady-state operations are anticipated.

12.4

Interpreting Results After data extraction, the most important aspect of PI analysis and optimization is the correct interpretation of results. These results are typically presented in the form of a printout generated by some software tool; in most cases, the software output is in the form of a grid diagram (e.g., STAR, 2009) or PFD supported by printout tables—as with ASPEN (AspenTech, 2009a, 2009b, 2009c) and gPROMS (PSE, 2009). In order to minimize typos and misinterpretation, many software tools feature an interface that facilitates the transfer of data files. This technology is now fairly well developed. The most challenging aspect of data interpretation is assessing the results in terms of possible further development or correction of the important process features. The interpretation will depend on the extent to which the factors mentioned previously (i.e., data uncertainty, data softness, flexibility, operability, controllability, safety, availability, and maintenance) have already been incorporated into the data extraction. If the data extraction did not reflect these considerations, then they must be addressed during the data interpretation. At this stage, the close collaboration of a team that includes the main involved professionals is highly recommended. Designers are strongly advised not to stick with just one solution but rather to explore different potential scenarios associated with various operating conditions and then test their design’s sensitivity to the possible variations. For screening and scoping it is helpful to use all types of Composite Curves as well as information (if provided by software) on which streams are contributing to specific parts of the curves.

12.5 Making It Happen Even when a sustainable and near-optimum design is developed, it must still be put into practice. This involves selling the

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Chapter Twelve proposals—which are often unconventional—to plant management, investors, and contractors. This was a big problem when PI was just beginning, and great strides in this area were made by UMIST, Bodo Linnhoff, and his company Linnhoff March in the 1980s and 1990s. PI has since proven itself and gained in popularity, so decision makers have become more receptive. Much of the situation’s improvement is due to multinational companies that have incorporated PI into their design and operational practice. Because the methodology has become widespread, it is not possible to list all of these companies. However, among the pioneers were members of the UMIST and, after the merger, the University of Manchester Process Integration Research Consortium: Air Products, Aspen, BASF, Bayer, BOC, BP, Canmet, Degussa, EDF, Engineers India, Exxon Mobil, Hydro, IFP, JGC, KBC, Mitsubishi Chemical Corporation, MOL, MW Kellogg, Petrobras, Petroleum Research Centre, Petrom, Petronas, Saudi Aramco, Shell, Sinopec, Technip, Total, UOP, and Vito. These firms were joined in the consortium by several universities, including University POLITEHNICA Bucharest and Petronas Technological University. There have also been strong supporters of PI in the United States, both at universities and in the industry; some of them are listed in Chapter 13. A major goal remains a close collaboration and smooth joint effort among PI specialists and the designers, managers, and owners (or contractors) of processing plants. A project’s best chance of success is when all these stakeholders share the goal of developing an optimized and sustainable process.

CHAPTER

13

Information Sources and Further Reading

T

here are various sources of information on optimization and integration in the process industry. The aim of this chapter is to summarize many of these sources, although their number is growing rapidly. No such list could be fully comprehensive, but every attempt has been made to include the most important sources of information. The chapter is divided into five sections as follows: (1) general sources of information, (2) Heat Integration, (3) Mass Integration, (4) combined analysis, and (5) optimization for sustainable industry. Within each section, listings are further divided into four groups: conferences, journals, service providers, and projects. A listing is repeated when the information is relevant to more than one category; this makes searching more efficient for users.

13.1

General Sources of Information 13.1.1

Conferences

Conferences that address Process Integration (PI) approaches to minimizing the use of energy, water, and other resources can be sorted into three groups. The first group consists of conferences that are directly related to energy and resource minimization. • Process Integration, Modelling and Optimisation for Energy Saving and Pollution Reduction (PRES), organized annually since 1998, • European Symposium on Computer Aided Process Engineering (ESCAPE), organized annually since 1992,

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Chapter Thirteen • AIChE International Congress on Sustainability Science and Engineering (ICOSSE), organized since 2009, • Dubrovnik Conference on Sustainable Development of Energy, Water and Environment Systems (SDEWES), organized biannually since 2002, • Italian Conference on Chemical and Process Engineering (ICheaP), organized biannually since 1993, • Europe Energy Efficiency Conference, The second group includes large conferences organized throughout the world and for which PI topics are part of their scientific programs. • AIChE annual and spring meetings, specialty conferences, and cosponsored conferences, • European Congress of Chemical Engineering (ECCE), organized biennially • Chemical Engineering, Chemical Equipment Design and Automation (CHISA), organized biennially since 1962 (odd years), • World Congress of Chemical Engineering, (the 9th World Congress of Chemical Engineering, incorporating the 14th APCChE Congress, will be held in 2013) • World Bioenergy, • World Sustainable Energy Days, • World Renewable Energy Congress: Innovation in Europe,

The third group of conferences includes those dealing with specific issues (food processing, pulp and paper, etc.) and at which energy and resource efficiency are addressed as special cases. • Total Food, organized biennially, • TAPPI EPE (Engineering, Pulping and Environmental) Conference, organized annually, • CLIMA Congress, official congress of the Federation of European Heating and Air-Conditioning Societies (REHVA),

Information Sources and Further Reading

13.1.2

Journals

There are many journals that cover topics related to energy, water, and resource minimization from the Process Integration standpoint; just a few of them are listed (alphabetically) here. • Chemical Engineering Transactions, • Journal of Clean Technologies and Environmental Policy, • Journal of Cleaner Production, • Resources, Conservation & Recycling,

13.1.3

Service Providers

The following alphabetical list includes service providers as well as professional bodies and networks. • ADAS, Inside and Solutions, Woodthorne, Wergs Rd., Wolverhampton, WV6 8TQ, UK, • Artie McFerrin Department of Chemical Engineering, Texas A&M University, College Station, TX 77843, USA, , contact person: Mahmoud M. El-Halwagi • AspenTech, Aspen Technology, Inc., 200 Wheeler Rd., Burlington, MA 01803, USA, • Dansk Energi Analyse A/S, • Department of Chemical Engineering, Auburn University, 212 Ross Hall, Auburn University, AL 36849-5127, USA, • BIS, Department for Business, Innovation and Skills, UK,

• Centre for Advanced Process Decision-Making, Carnegie Mellon University, Department of Chemical Engineering, 5000 Forbes Ave., Pittsburgh, PA 15213, USA, • Center for Engineering and Sustainable Development Research, De La Salle University, Manila, 2401 Taft Avenue, 1004 Manila, Philippines, , contact person: Raymond Tan • Centre for Process Integration, School of Chemical Engineering and Analytical Science, The University of

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Chapter Thirteen Manchester (formerly UMIST), Manchester, M13 9PL, UK, , contact person: Robin Smith • Centre for Process Integration and Intensification (CPI2), European Community Project Marie Curie Chair (EXC) MEXC-CT-2003-042618 INEMAGLOW, Research Institute of Chemical and Process Engineering, Faculty of Information Technology, University of Pannonia, Egyetem u.10, Veszprem, H-8200, Hungary, , contact person: Jiří Klemeš • Centre for Process Systems Engineering, Imperial College London, C507 Roderic Hill Bldg., South Kensington Campus, London, UK, , contact person: Efstratios Pistikopoulos • Centre for Technology Transfer in the Process Industries, University POLITEHNICA Bucharest, 1 Polizu St., Bldg. A, RO-011061, Bucharest, Romania, , contact person: Valentin Pleşu • Charles Parsons Institute, University of Limerick, Limerick, Ireland, , contact person: Toshko Zhelev • Chiyoda Corporation, Energy Frontier Business Development Office, 2-12-1 Tsurumichuo, Tsurumi-ku, Yokohama 230-8601, Japan, , contact person: Kazuo Matsuda • COWI A/S, Parallelvej 2, DK-2800, Kongens Lyngby, Denmark, tel. +45 45 97 22 11, , [email protected] • DEFRA, Department for Environment, Food and Rural Affairs, UK, • Department of Chemical and Environmental Engineering, University of Nottingham Malaysia, Broga Rd., 43500 Semenyih, Selangor, Malaysia, , contact person: Dominic Foo • Department of Chemical Engineering, University of Maribor, Smetanova ulica 17, Maribor, Slovenia, , contact person Zdravko Kravanja • Department of Chemical Engineering, Massachusetts Institute of Technology, 77 Massachusetts Ave., Room 66–350, Cambridge, MA 02139, • Department of Chemical Engineering, University of Pretoria, Lynwood Rd., Pretoria 0002, South Africa, , contact person: Thoko Majozi • Department of Computer Science and Systems Technology, Faculty of Information Technology, University of Pannonia, Egyetem u.10, Veszprem, H-8200, Hungary, , contact person: Ferenc Friedler • Department of Energy and Climate Change, UK, • Department of Energy and Environment, Chalmers University of Technology, SE-412 96, Göteborg, Sweden, , contact person: Thore Berntsson • Energy Information Administration, USA, • Energy Research Group, School of Science & Engineering, University of Waikato, Hamilton 3240, New Zealand, , contact person: Martin Atkins • Energy Science and Engineering, Indian Institute of Technology Bombay, Powai, Mumbai, 400076, India, , contact person: Santanu Bandyopadhyay • European Integrated Pollution Prevention and Control Bureau, producing best available techniques (BAT) reference documents (aka BREFs), • EVECO Brno, Březinova 42, 616 00 Brno, Czech Republic, , contact person: Jaroslav Oral • Fraunhofer Institute for Environmental, Safety and Energy Technology (UMSICHT), Osterfelder Str., D-46047, Oberhausen, Germany, • Global Footprint Network (“Advancing the Science of Sustainability”), 312 Clay St., Suite 300, Oakland, CA 946073510, USA, , contact person: Susan Burns • Institute for Scientific Research, University of Guanajuato, Lascurain de Retana No 5, 36000, Guanajuato, Gto., México, , contact person: Martin Picon-Nuñez • Institute of Process and Environmental Engineering, Faculty of Mechanical Engineering, Brno University of Technology (UPEI VUT), Brno, Technická 2896/2, 616 69, Brno, Czech Republic, , contact person: Petr Stehlík

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Chapter Thirteen • International Energy Agency, 9 rue de la Fédération, 75739 Paris Cedex 15, France, , contact persons: Nobuo Tanaka (Executive Director); Richard H. Jones (Deputy Executive Director) • KBC Energy Services (formerly Linnhoff March), Targeting House, Gadbrook Park, Northwich, Cheshire CW9 7UZ, UK,

• Laboratory for Industrial Energy Systems, Ecole Polytechnique Federale de Lausanne, Bat. ME A2, Station 9, CH-1015 Lausanne, Switzerland, , contact person: Francois Marechal • Lehrstuhl für Technische Chemie A, Technische Universität Dortmund, Fakultät Bio- und Chemieingenieurwesen, Geschossbau 1, Emil-Figgestr. 66, 44227, Dortmund, Germany,

• Mechanical Engineering Faculty, Universität Paderborn, Warburger Str. 100, D-33098, Paderborn, Germany, • Process Integration Ltd, One Central Park, Northampton Road, Manchester, M40 5WW, UK, , contact person: Robin Smith • Scottish Environment Protection Agency (SEPA), • AO Sodrugestvo-T, NTU ‘KhPI’, Frunze Str., 21, 61002, Kharkov, Ukraine, • Thermal Energy, Department of Energy and Process Engineering, Norwegian University of Science and Technology, NO-7491, Trondheim, Norway, , contact person: Truls Gundersen • UK Energy Research Centre, 58 Princes Gate, Exhibition Rd., London SW7 2PG, UK, • University College London Energy Institute, Central House, 14 Upper Woburn Place, London, WC1H 0HY, UK, • U.S. Department of Energy, USA, • U.S. Environmental Protection Agency, National Risk Management Research Lab/USEPA, 26 W. M.L. King Dr., Cincinnati, OH 45268, USA, , contact person: Subhas K. Sikdar • Warsaw University of Technology, Płock Campus, Warsaw, Poland, , contact person: Krzysztof Urbaniec

Information Sources and Further Reading

13.1.4

Projects

There have been hundreds of projects related to these general concerns. Several typical projects that are publicly available are listed in subsequent sections dealing with specific applications (13.2.4, 13.3.4, 13.4.4, 13.5.4).

13.2

Heat Integration 13.2.1

Conferences

• Process Integration, Modelling and Optimisation for Energy Saving and Pollution Reduction (PRES), organized annually since 1998, • Dubrovnik Conference on Sustainable Development of Energy, Water and Environment Systems (SDEWES), organized biennially since 2002, • Italian Conference on Chemical and Process Engineering (ICheaP), organized biannually since 1993,

13.2.2

Journals

• Applied Thermal Engineering, • Energy, • Heat Transfer Engineering, • Renewable Energy,

13.2.3

Service Providers

• American Process Inc., 817 West Peachtree St., Suite M105, Atlanta, GA 30308, USA [also offices in Athens (Greece), and Cluj-Napoca (Romania)], , contact person: Theodora Retsina • Artie McFerrin Department of Chemical Engineering, Texas A&M University, College Station, TX 77843, USA, , contact person: Mahmoud M. El-Halwagi • Centre for Process Integration, School of Chemical Engineering and Analytical Science, The University of Manchester (formerly UMIST), Manchester, Oxford Rd., M13 9PL, UK, , contact person: Robin Smith • Centre for Process Integration and Intensification (CPI2), Research Institute of Chemical and Process Engineering, Faculty of Information Technology, University of Pannonia, Egyetem u.10, Veszpréem, H-8200, Hungary, , contact person: Jiří Klemeš • Charles Parsons Institute, University of Limerick, Limerick, Ireland, , contact person: Toshko Zhelev • Chemical Process Engineering Research Institute (CPERI), Center for Research and Technology-Hellas (CERTH), PO Box 361,Thermi Thessaloniki, Greece, • Department of Chemical and Biochemical Engineering, Technical University of Denmark (DTU), Søltofts Plads, Bldg. 229, DK-2800 Kgs. Lyngby, Denmark, • Department of Chemical and Process Engineering, Rzeszow University of Technology, al. Powstańców Warszawy 6, 35–959 Rzeszów, Poland, , contact person: Jacek Jeżowski • Department of Chemical Engineering, University of Monash, PO Box 36, Clayton, Victoria 3800, Australia, • Department of Energy and Environment, Chalmers University of Technology, SE-412 96, Göteborg, Sweden, , contact person: Thore Berntsson • Energy Research Group, School of Science & Engineering, University of Waikato, Hamilton 3240, New Zealand, , contact person: Martin Atkins • Energy Science and Engineering, Indian Institute of Technology Bombay, Powai, Mumbai, 400076, India, , contact person: Santanu Bandyopadhyay • EVECO Brno, Březinova 42, 616 00 Brno, Czech Republic, , contact person: Jaroslav Oral • Faculty of Technology, Lappeenranta University of Technology, P.O.Box 20, FIN-53851 Lappeenranta, Finland,

• Institute of Process and Environmental Engineering, Faculty of Mechanical Engineering, Brno University of Technology

Information Sources and Further Reading (UPEI VUT), Brno, Technická 2896/2, 616 69, Brno, Czech Republic, Contact person: Petr Stehlík, , contact person: Petr Stehlík • KBC Energy Services (formerly Linnhoff March), Targeting House, Gadbrook Park, Northwich, Cheshire CW9 7UZ, UK,

• Laboratory for Analysis and Synthesis of Chemical Systems, Institut de Chimie-Bâtiment B6, Sart Tilman, 4000 Liège, Belgium, • Laboratory for Industrial Energy Systems, Ecole Polytechnique Federale de Lausanne, Bat. ME A2, Station 9, CH-1015 Lausanne, Switzerland, , contact person: Francois Marechal • Process Design Center (PDC), B.V. Catharinastraat 21f, NL-4811 XD Breda, The Netherlands, • Process Integration Ltd, One Central Park, Northampton Road, Manchester, M40 5WW, UK, , contact person: Robin Smith • AO Sodrugestvo-T, NTU ‘KhPI’, Frunze Str., 21, 61002, Kharkov, Ukraine, • Thermal Energy, Department of Energy and Process Engineering, Norwegian University of Science and Technology, NO-7491, Trondheim, Norway, , contact person: Truls Gundersen • U.S. Environmental Protection Agency, National Risk Management Research Lab/USEPA, 26 W. M.L. King Dr., Cincinnati, OH 45268, USA, , contact person: Subhas K. Sikdar • VTT Technical Research Centre of Finland, PO Box 1000, FI02044 VTT, Finland, • Warsaw University of Technology, Płock Campus, Warsaw, Poland, , contact person: Krzysztof Urbaniec

13.2.4

Projects

• TOTAL SITE, European Community Non-Nuclear Energy Programme Research & Technology Development Project JOULE II PL920520, “Targeting and Planning for Reduction of Fuel, Power and CO2 on Total Sites” • EMINENT 2, “Early Market Introduction of New Energy Technologies in Liaison with Science and Industry,”

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Chapter Thirteen • EUBIONET 3, “Solutions for Biomass Fuel Market Barriers and Raw Material Availability,” • PEPNET, “Network for the Promotion of RTD Results in the Field of Eco-building Technologies, Small Polygeneration and Renewable Heating and Cooling Technologies for Buildings,” • European Community Project JOULE II PL930287, “Methodology for Optimisation of Operation Site-Scale Energy Used in Production Plants” • European Community Project JOULE II PL 930485, “Process Integration with Combined Heat and Power” • U.S. Environmental Protection Agency, Ernest Orlando Lawrence Berkeley National Laboratory, “Energy Efficiency Improvement and Cost Saving Opportunities for Petroleum Refineries, An ENERGY STAR Guide for Energy and Plant Managers” (by E. Worell & C. Galitsky), LBNL-56183 • U.S. Department of Energy, Office of Energy Efficiency and Renewable Energy, “Ultra-Low-Emission, Integrated Process Heater System,” , accessed 22 December 2009; Bob Gremmer, High-Efficiency Technology Manager, 1000 Independent Avenue SW, Washington, DC 20585, USA • “Development of an Advanced Combined Heat and Power (CHP) System Utilizing Off-Gas from Coke Calcination, Utilization of Process Off-Gas as a Fuel for Improved Energy Efficiency,” , accessed 22 December 2009; project partners: Yaroslav Chudnovsky, Gas Technology Institute (GTI), Des Plaines, IL; Mark Zak, Superior Graphite Co. (SGC), Chicago, IL

13.3

Mass Integration 13.3.1

Conference

• Loss Prevention and Safety Promotion in the Process Industries, organized triennially,

13.3.2

Journals

• Journal of Clean Technologies and Environmental Policy,

Information Sources and Further Reading • Journal of Cleaner Production, • Resources, Conservation & Recycling, • Transactions of the IChemE, UK

13.3.3

Service Providers

• American Process Inc., 817 West Peachtree St., Suite M105, Atlanta, GA 30308, USA, [also offices in Athens (Greece) and Cluj-Napoca (Romania)], , contact person: Theodora Retsina • Artie McFerrin Department of Chemical Engineering, Texas A&M University, College Station, TX 77843, USA, , contact person: Mahmoud M. El-Halwagi • Centre for Process Integration, School of Chemical Engineering and Analytical Science, The University of Manchester (formerly UMIST), Manchester, Oxford Rd., M13 9PL, UK, , contact person: Robin Smith • Centre for Process Integration and Intensification (CPI2), European Community Project Marie Curie Chair (EXC) MEXC-CT-2003–042618 INEMAGLOW, Research Institute of Chemical and Process Engineering, Faculty of Information Technology, University of Pannonia, Egyetem u.10, Veszprem, H-8200, Hungary, , contact Person: Jiří Klemeš • Charles Parsons Institute, University of Limerick, Limerick, Ireland, , contact person: Toshko Zhelev • Department of Chemical Engineering, University of Monash, PO Box 36, Clayton, Victoria 3800, Australia, • KBC Energy Services (formerly Linnhoff March), Targeting House, Gadbrook Park, Northwich, Cheshire CW9 7UZ, UK,

• Process Integration Ltd, One Central Park, Northampton Road, Manchester, M40 5WW, UK, , contact person: Robin Smith • School of Chemical and Environmental Engineering, University of Nottingham Malaysia, Broga Rd., 43500

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Chapter Thirteen Semenyih, Selangor, Malaysia, , contact person: Dominic Foo • VTT Technical Research Centre of Finland, PO Box 1000, FI02044 VTT, Finland, • Water Footprint Network, University of Twente, UNESCOIHE, RIVM, , contact person: A.Y. Hoekstra

13.3.4

Projects

• “Assessing Collaborative and Integrated Water Management in the Maitland River Watershed,” University of Guelph, Ontario, Canada, • European Community Programme JOULE III PL950749, “Water Pinch: Simultaneous Energy and Water Use Minimisation” • AWARNET (Agro-food Wastes Minimisation and Reduction Network), project involving various aspects of waste minimization and energy, EC GROWTH, GRD1-CT2000-28033 (de las Fuentes, Sanders, and Klemeš, 2002), , accessed 10 December 2005 • EU INCO Project ERB IC18-CT98-0271, “Intelligent Management System for Water and Energy Minimisation in Latin American Food Industries – WATERMAN” • “Waste Minimisation for the Process Industry: New Researchers’ Fund,” University of Nottingham Malaysia, May 2006–April 2009

13.4

Combined Analysis 13.4.1

Conferences

• Process Integration, Modelling and Optimisation for Energy Saving and Pollution Reduction (PRES), organized annually since 1998, • Italian Conference on Chemical and Process Engineering (ICheaP), organized biannually since 1993,

Information Sources and Further Reading

13.4.2

Journals

• Applied Thermal Engineering, • Chemical Engineering and Processing, • Chemical Engineering Science, • Chemical Engineering Transactions, • Computer Aided Chemical Engineering, • Ecological Modelling, • Energy, • Journal of Clean Technologies and Environmental Policy, • Journal of Cleaner Production, • Renewable Energy, • Resources, Conservation & Recycling, • Waste Management,

13.4.3

Service Providers

• AspenTech, Aspen Technology, Inc., 200 Wheeler Rd., Burlington, MA 01803, USA, • Centre for Process Integration, School of Chemical Engineering and Analytical Science, The University of Manchester (formerly UMIST), Manchester, Oxford Rd., M13 9PL, UK, , contact person: Robin Smith • Centre for Process Integration and Intensification (CPI2), European Community Project Marie Curie Chair (EXC)

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Chapter Thirteen MEXC-CT-2003-042618 INEMAGLOW, Research Institute of Chemical and Process Engineering, Faculty of Information Technology, University of Pannonia, Egyetem u.10, Veszprém, H-8200, Hungary, , contact Person: Jiří Klemeš • Charles Parsons Institute, University of Limerick, Limerick, Ireland, , contact person: Toshko Zhelev • Department of Chemical Engineering, University of Massachusetts, Amherst, MA, USA, • Hebling Technik, Hohlstr. 614, CH-8048 Zurich, Switzerland,

• Process Integration Ltd, One Central Park, Northampton Road, Manchester, M40 5WW, UK, , contact person: Robin Smith • School of Chemical and Environmental Engineering, University of Nottingham Malaysia, Broga Rd., 43500 Semenyih, Selangor, Malaysia, , contact person: Dominic Foo

13.4.4 Projects • AVICENNE, “Integrated Concept for the Fermentation of Sewage Sludge and Organic Waste as a Source of Renewable Energy and for Use of the Fermented Products as a Hygienic Fertiliser and Soil Improver,” AVI*94005, Universität Stuttgart, Germany, 1997 • ANDI-POWER-CIFRU, “An Anaerobic Digestion Power Plant for Citrus Fruit Residues,” FP5 EESD NNE5/364/ 2000, Envisec S.A., Greece, 2004, , accessed 14 March 2006 • Biogas by Bioaugment, “Optimized Biogas Production and Resource Recovery through Bio-Augmentation in a Joint Plant Treating Poultry and Pig Waste,” NNE5/46/1999, Centro para a Conservaçao de Energia, Praceta 1, 2720-537 Amadora, Portugal, , accessed 14 March 2006 • DEP-PROJECT, “Power Plant Based on Fluidized Bed Fired with Poultry Litter,” FP5 NNE5/75/1999, 2003, Energy Systems BV, De Vest 51, Postbus 218, 5555 XP Valkenswaard,

Information Sources and Further Reading Netherlands, , accessed 14 March 2006 • “Development of a CHP Process Using Grease and Oil Waste from Plants and Animals,” FP5 EESD ENK5 CT-2000-35008, Sud recuperation Sarl, France, 2001, , accessed 14 March 2006 • “Development of Property Integration Techniques for Waste Minimisation,” Ministry of Science, Technology and Innovation, Malaysia University of Nottingham Malaysia, September 2007–August 2009 • INEMAGLOW European Community Project MARIE CURIE CHAIR (EXC) MEXC-CT-2003-042618 “Integrated Waste to Energy Management to Prevent Global Warming”, • Project SUCLEAN, “Research on Minimization of Energy and Water Use in Sugar Production by Cooling Crystallization of Concentrated Raw Juice,” IC15960734, , accessed 10 December 2005 • WREED, “Development of an Energy Efficient to Reduce the Cost of Drying Food and Feed Waste,” FP5 EESD ENK6CT2001-30002, Ceramic Drying Systems Ltd, UK, 2004, , accessed 3 May 2010 • “Western Renewable Energy Zones,” a joint initiative of the Western Governors’ Association and U.S. Department of Energy, , accessed 29 December 2009 • “Flexible Distributed Energy and Water from Waste for the Food and Beverage Industry,” General Electric, , accessed 29 December 2009

13.5 Optimization for Sustainable Industry 13.5.1

Conferences

• AIChE meetings, organized twice annually in the United States,

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Chapter Thirteen • European Symposium on Computer Aided Process Engineering (ESCAPE), organized annually since 1992, • AIChE International Congress on Sustainability Science and Engineering (ICOSSE), organized since 2009,

13.5.2

Journals

• AIChE Journal, • Chemical Engineering and Processing, • Chemical Engineering Science, • Chemical Engineering Transactions, • Computers & Chemical Engineering, • Industrial & Engineering Chemistry Research, • Journal of the Chinese Institute of Chemical Engineers, • Journal of Universal Computer Science,

13.5.3

Service Providers

• Advanced Process Combinatorics, Inc., Purdue Technology Center, 3000 Kent Ave., West Lafayette, IN 47906, USA,

• AspenTech, Aspen Technology, Inc., 200 Wheeler Rd., Burlington, MA 01803, USA, • Centre for Process Systems Engineering, Imperial College London, C507 Roderic Hill Bldg., South Kensington Campus, London, UK, , contact person: Efstratios Pistikopoulos • Computer-Aided Systems Laboratory, Department of Chemical Engineering, Princeton University, Princeton, NJ 08544 USA, , Contact person Christodoulos A. Floudas • Department of Computer Science and Systems Technology, Faculty of Information Technology, University of Pannonia,

Information Sources and Further Reading Egyetem u.10, Veszprém, H-8200, Hungary, , contact person: Ferenc Friedler • Honeywell, 300-250 York St., London, Ontario, N6A 6K2 Canada, • Laboratory for Industrial Energy Systems, Ecole Polytechnique Federale de Lausanne, Bat. ME A2, Station 9, CH-1015 Lausanne, Switzerland, , contact person: Francois Marechal • Process Integration Ltd, One Central Park, Northampton Road, Manchester, M40 5WW, UK, , contact person: Robin Smith • School of Chemical Engineering, Purdue University, Forney Hall of Chemical Engineering, 480 Stadium Mall Dr., West Lafayette, IN 47907, • U.S. Environmental Protection Agency, National Risk Management Research Lab/USEPA,26 W. M.L. King Dr., Cincinnati, OH 45268, USA, , contact person: Heriberto Cabezas

13.5.4

Projects

• ZEROWIN, “Towards Zero Waste in Industrial Networks,” Austrian Society for Systems Engineering and Automation, Gurkgasse 43/2, A-1140 Vienna, Austria, • EMINENT 2, “Early Market Introduction of New Energy Technologies in Liaison with Science and Industry,” • PRISM, “Knowledge-Based Processing Systems,” FP6 MC Human Resources Project (Prof. E. Pistikopoulos, coordinator), Imperial College of Science Technology and Medicine, London, UK,

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CHAPTER

14

Conclusions and Further Information

T

he two options when writing this book were either to make it fully comprehensive or to present selected material while directing the reader to sources of further information. The first option would have resulted in a book of more than a thousand pages, so it was decided to keep the book compact and thus accessible to a wider audience. This chapter supplies additional references to provide guidelines for more detailed and comprehensive studies.

14.1

Further Reading Chapter 13 gives an overview of places to find more information. Of course, the most recent information is found in archive research papers and proceedings from related conferences. However, the number of research papers has been increasing, and many of them are dedicated to rather specialized matters. For this reason, it is often useful for a potential user of the methodology to have some material for further reading: guidebooks, handbooks, and teaching texts. The reader should bear in mind that even the most excellent books are only as current as their date of publication. No book can cover methodology developed subsequent to its printing.

14.1.1

Books and Key Articles

Process Integration The most well-known and perhaps most referenced book on Process Integration (PI) is A User Guide on Process Integration for the Efficient Use of Energy (Linnhoff et al., 1982). This “red book,” authored by a team led by Bodo Linnhoff, was updated for an extended second edition in 1994. Although it was published a long time ago, it remains an excellent vehicle for teaching and learning about Heat Integration and several other PI applications, providing the reader with a smooth and understandable learning path.

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Chapter Fourteen Valuable references for engineers (as well as for teachers and students) are the books authored by Robin Smith, Linnhoff’s successor to head of the Department of Process Integration at UMIST and—after the university merged to become the University of Manchester—director of the Centre for Process Integration. Smith published two books: the first in 1995 and a new version in 2005 that included more recent developments. Ian Kemp undertook the task of developing the second (1994) edition of Linnhoff’s red book, and in 2007 he published an updated and extended version. Some of UMIST legacy course materials (CPI, 2004 and 2005) were used in that book (Kemp, 2007), which also includes spreadsheet software available as a web annex. A handy guidebook entitled A Process Integration Primer was developed by Gundersen (2000) with support from the International Energy Agency. Shenoy (1995) described the application of Heat Integration methodology to Heat Exchanger Network synthesis. Furman and Sahinidis (2002) presented a comprehensive review of 461 published works (through the year 2000) on heat exchanger synthesis, although this article is rife with misspelled non-English names (e.g., “Klemeš” was rendered as “Klemebvs”). More recently, Sieniutycz and Jeżowski (2009) authored a book dedicated to PI and energy optimization methods. In addition, a number of books (and chapters of books) have resulted from the collaboration between Centre for Process Integration at the University of Manchester and a Centre for Process Integration and Intensification (CPI2), recently created at the University of Pannonia. Key staff members of CPI2 gained much of their experience at UMIST, and the two centers have been close collaborators. Chapters have been published in handbooks related to energy and to the management of water and waste in food processing, and the material provided includes advanced methodology in addition to a number of case studies. This material can be found in Klemeš and Perry (2007a, 2007b) and in Klemeš, Smith, and Kim (2008). The water footprint’s connection to water integration was examined in a chapter from Klemeš, Varbanov, and Lam (2009), and combining PI with state-of-the-art methods for the recovery of organic materials from process water in the food industry was discussed by Napper, Kim, and Bulatov (2009) in their chapter of that same handbook. Carbon footprint and its relation to energy efficiency are analyzed in a chapter of Klemeš, Bulatov, and Perry (2008). Substantial developments in the field of mass integration have been reported by Mahmud El-Halwagi and colleagues; in particular, the synthesis of mass exchange networks (MENs) was reviewed by El-Halwagi (1997, 1999), El-Halwagi and Spriggs (1998), and Spriggs and El-Halwagi (2000). This information is also available in the book

Conclusions and Further Information form (El-Halwagi, 2006). A fast-developing group at the Malaysian campus of the University of Nottingham has compiled a new book edited by Dominic Foo and his colleagues (Foo, El-Halwagi, and Tan, 2010). An overview of capital cost targeting for MEN synthesis was provided by Fraser and Hallale (2000a, 2000b), and the application of Mathematical Programming to MEN synthesis was reviewed by Galan and Grossmann (1999) and Grossmann, Caballero, and Yeomans (1999).

Optimization and Optimal Design of Industrial Processes Several books covering these topics were published in the late 1980s and the 1990s. Although much time has passed since then, the basics of optimization are still valid. Texts that are worth mentioning include Conceptual Design of Chemical Processes (Douglas, 1988), Nonlinear and Mixed-Integer Optimization: Fundamentals and Applications (Floudas, 1995), and Systematic Methods of Chemical Process Design (Biegler, Grossman, and Westerberg, 1997). The book by Bumble (1999) also provides useful information. A series of books have been published on process system engineering, including titles by Seferlis and Georgiadis (2004), Papageorgiou and Geogiadis (2007a, 2007b), Pistikopoulos, Georgiadis, and Dua (2007a, 2007b), and Georgiadis, Kikkinides, and Pistikopoulos (2008). Along with extensive information on process costing, the wellknown Plant Design and Economics for Chemical Engineers (Peters, Timmerhaus, and West, 2003) contains a wealth of knowledge on optimization methodologies, including P-graph basics.

14.1.2 Lecture Notes and Online Teaching Resources Teaching materials and training courses covering the various aspects of PI have been developed for many years at UMIST and The University of Manchester. These materials are based on more than 25 years research and are continuously updated by the Process Integration Research Consortium. The material has been used as a basis for a number of books in the field; for example, some of it was referenced in CPI (2004 and 2005). It also has been supported by such PI software as SPRINT (2009), STAR (2009), WATER (2009), and WORK (2009). The training courses were closely developed with Linnhoff March (1998) to produce Introduction to Pinch Technology, which later developed independently. Another well-known source of teaching materials is A Process Integration Primer (Gundersen, 2000), which provides a comprehensive overview of the period up to year 2000. Teaching materials are also included in Energy and Process Integration (Georgiadis and Pistikopoulos, 2006). Many other teaching resources have either been developed in-house or been tailor-made for specific fields such as the pulp and paper industry, oil refining industry, and the sugar industry.

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Chapter Fourteen

Development Trends At the 2009 PRES conference, development trends in PI, optimization, and Mathematical Programming as tools for sustainability in process industries were reviewed by Friedler (2009, 2010). Some of these trends are discussed in this section.

14.2.1

Top-Level Analysis

A typical industrial site comprises different process production units linked to a common utility system. The centralized utility system meets the demands for heat and power, creating indirect links between the processes. Considerable amounts of steam can often be saved by optimizing and retrofitting site processes and their heat exchanger networks (Dhole and Linnhoff, 1993a; Asante and Zhu, 1997). Although such projects might have the potential to save steam at different pressure levels, they may not always save costs or even fuel. Moreover, steam at a given level of pressure can have different prices depending on how much is saved, despite the common practice of attributing a single value to steam at a given level. This issue was first addressed systematically by Makwana and colleagues (Makwana, 1998; Makwana, Smith, and Zhu, 1998), who provided an approach to screening energy projects without the need to collect data from every site process. Instead, their methodology of top-level analysis required the collection and analysis only of basic data relating to the central utility system. This approach was based on comparing current and optional heat flow paths through the utility system. The procedure provided a good conceptual view of the problem, but the required number of manual steps and calculations was not amenable to automation and too complex for application to real sites. However, an important concept derived from this initial version of top-level analysis is that, given marginal steam prices, a small part of the total site can be analyzed to rank the most promising directions for steam-saving projects. Those marginal steam prices are key because they can be computed in a different way—namely, by utility system optimization. This approach led to the development by Varbanov et al. (2004) of a stepwise optimization procedure that can be used to determine the true marginal price of steam at different pressure levels as well as the constraints on steam savings imposed by the utility system. This approach builds on the optimization framework for industrial utility systems presented by Varbanov, Doyle, and Smith (2004), and it enables the analysis of complex utility systems using automated tools for utility system optimization.

14.2.2 Maintenance Scheduling, Maintainability, and Reliability A chief concern of companies and operators is that industrial plants should operate safely and reliably, with minimal costs for maintenance.

Conclusions and Further Information Increasing the efficiency of process systems via PI increases the importance of this issue because PI also increases the interdependence of the various process modules and subsystems. Cheung and Hui (2004) proposed a scheme for Total Site maintenance scheduling for better energy utilization. To minimize the impacts on production and utility systems during routine maintenance, the scheduling must be done carefully and with consideration of sitewide utilities and material balances. The reliability analysis targets maintenance requirements, cost, availability, and maintainability. The methodology described by Yin et al. (2009) considers flexible process design simultaneously with reliability and risk factors, and the best solutions are obtained by optimizing the PI. Sikos and Klemeš (2010a, 2010b) applied a combination of HEN optimization and reliability software packages to develop a methodology with several advantages over the commonly used approach.

14.2.3

Hybrid Energy Conversion Systems

Energy conversion systems for heat and power generation traditionally involve only gas and steam turbines. However, the interest of research and industrial engineers has recently been attracted by a broader range of technologies: the hybrid energy conversion systems involving fuel cells (FCs). Especially interesting are high-temperature fuel cells (HTFCs), which feature electrical efficiency of 40–60 percent (Yamamoto, 2000) compared with 30–35 percent for most gas turbines (Gas Turbine World, 2001). There has been an extensive research aimed at improving the efficiency of FC systems. Karvountzi, Price, and Duby (2004) compared the integration of molten carbonate fuel cells (MCFCs) and solid oxide fuel cells (SOFCs) into hybrid systems. Kurz (2005) focused on the choice of appropriate gas turbines for the given FCs, and Massardo and Bosio (2002) studied the MCFC combinations with gas and steam turbines. One promising option is to integrate the FCs with “bottoming cycles” for dedicated power generation or Combined Heat and Power applications. Varbanov et al. (2006) and Varbanov and Klemeš (2008) studied the benefits of integrating HTFC systems with steam cycles for purposes of industrial cogeneration. The results indicate that HTFCs have great potential in terms of economic viability and a low carbon footprint.

14.2.4 Integration of Renewables and Waste Most energy systems of industrial, residential, service and business, agriculture, and production sites continue to use fossil fuels as their primary energy source. Sites are usually equipped with steam and/ or gas turbines and with steam boilers and water heaters (running on electricity or gas) as energy conversion units. The challenge of increasing the share of renewables in the primary energy mix could be met by integrating solar, wind, biomass, and some types of waste

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Chapter Fourteen with the fossil fuels. Renewable resources typically feature availability distributed over certain areas, varying significantly with time and location. Another source of variability is the energy demands (for heating, cooling, and power) of residential and business consumers, which vary significantly with the time of day and period of the year. (The notable exception is large-scale industries that operate continuous processes; in this case, variations are less pronounced and can often be either neglected or conveniently modeled using multiperiod optimization.) Furthermore, the variations in consumer energy demand are not synchronous but instead are displaced in time. For instance, commercial and office buildings tend to have higher energy demands during normal business hours, whereas residential demands tend to increase after business hours. These factors all make optimizing the design of energy conversion systems using renewable resources more complex than when using fossil fuels only. However, combining the supply and demand streams of individual users may allow such systems to serve industrial plants as well as residential customers and the service sector (hotel complexes, hospitals). The design task is to account for both the demand- and supply-side variability. One approach to solving the task is to employ advanced PI methodology with time as another problem dimension. A basic methodology along these lines has already been developed for Heat Integration of batch processes (Kemp and Deakin, 1989; Klemeš et al., 1994) and was recently revisited by Foo, Chew, and Lee (2008). A further important step in the direction of extending this methodology to Heat Integration of renewables was taken by Perry, Klemeš, and Bulatov (2008), who considered the integration of local energy sectors into extended total sites involving residential and commercial processes and buildings in addition to industrial ones. This work was further developed by Varbanov and Klemeš (2010) to account for the integration of inherently variable renewables. Converting waste via thermal processing is an intriguing option because it simultaneously reduces the demand for fossil fuels and landfilling. Bébar et al. (2001, 2002) demonstrated a method for efficiently utilizing the heat value of incineration products that would partially compensate for the cost of thermal waste treatment. The challenge of utilizing waste as an energy source is not variability, as it is with renewables, since waste is relatively plentiful and generated at significant rates. Rather, the main problems associated with extracting energy from waste are technological. Municipal and other solid wastes are typically incinerated (Bébar et al., 2001; Bébar et al., 2002; Stehlik, 2009), a process that involves three principal issues. First, the incineration must ensure efficient combustion and minimal emissions of pollutants; this is often achieved by co-firing

Conclusions and Further Information the waste with other fuels (Werther, 2007). Second, it is important to prevent the release of toxic pollutants with the flue gas—for example, the emission of dioxins from incinerated solid wastes. These emissions can be minimized by proper waste separation and moisture reduction prior to the incineration (Werther, 2007). Third, the moisture content poses other challenges besides the formation of dioxins. The higher the moisture content, the larger fraction of energy is wasted on evaporating it; thus, increased moisture reduces the specific energy gain from incineration. This means that, for purposes of energy generation, waste with especially high water content is more beneficially treated via other processes. Examples include the anaerobic digestion of wet organic waste from food industry and agriculture (Zhang et al., 2007; Macias-Corral et al., 2008) and the supercritical gasification of black liquor from pulpand-paper plants (Pettersson and Harvey, 2009; Sricharoenchaikul, 2009).

14.2.5 Better Utilization of Low-Grade Heat Desai and Bandyopadhyay (2010) proposed a scheme incorporating organic Rankine cycles (ORCs) in the efficient utilization of lowgrade waste heat for power generation. They provided a graphically assisted procedure for integrating an industrial process with an ORC, thereby reducing the process cooling demand and the need to import external power.

14.2.6

Energy Planning That Accounts for Carbon Footprint

The international community has become increasingly concerned with climate change. Most attention has been focused on the carbon footprint (CFP), which quantifies the impact of greenhouse gas emissions. In parallel with this development, the issue of energy independence has been given more attention in a number of countries that import fossil fuels—especially the United States, European countries (except Norway), and, to a lesser extent, Australia and Japan. An interesting paper by Foo, Tan, and Ng (2008) addresses “Carbon and Footprint-Constrained Energy Planning Using Cascade Analysis Technique.” The authors presented algebraic targeting techniques for energy-sector planning under constraints on CO2 emissions and land availability. This contribution extends the classic Pinch Analysis of Linnhoff and Hindmarsh (1983) to identify the minimum amount of low- or zero-carbon energy sources needed to meet regional or national energy demands while observing limits on CO2 emissions. The concept of Regional Energy Clustering presented by Lam, Varbanov, and Klemeš (2010) involves the synthesis of regional energy targeting and supply chains. The methodology seeks to account for

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Chapter Fourteen the complete spectrum of renewable energy sources and energy carriers—and to evaluate the appropriate combinations of waste-toenergy and fossil fuels—in order to deliver more complete and practical procedures.

14.3

Conclusions In recent years there has been much interest in the development of renewable, non-carbon-based energy sources to combat the threat of increased CO2 emissions and related climatic change. Increases in the price of oil and gas have further boosted interest in such alternative energy sources. These concerns have resulted in increased efficiency of energy and water use in the industrial sector, although the major industry’s use of renewable energy sources has been only sporadic. In contrast, domestic energy supply has moved more positively toward the integration of renewable energy sources, including wind turbines, solar heating, and heat pumps. Yet efforts to design a sustainable combined energy system that includes both industrial and residential buildings have been limited and ad hoc, since there are no systematic design techniques available for producing a symbiotic system on this scale. Increasing the efficiency of energy-using processes is the most effective current method for reducing costs and emissions that affect the stability of the world’s climate, and contributing to sustainable growth. Increasing energy efficiency is the cleanest short-term method to produce green energy—that is, energy that produces the least amount of emissions. The situation is similar with respect to minimizing the consumption of water and the generation of wastewater. Unfortunately, these relatively mundane approaches are often overlooked by those who are seduced by exciting new technologies—such as renewable energy sources—that have generated more publicity. Nonetheless, the primary sustainability issue remains the efficient use of resources: raw materials, energy, and water. Two metrics have recently been developed to assess the impact of energy-efficient methods and energy-reduction proposals. The carbon footprint (CFP) takes account of all carbon emissions over the entire life cycle of a process or product, and the water footprint (WFP) indicates how much water is used during the life cycle of a product or service.

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Index A ABB algorithm. See Accelerated Branch and Bound algorithm Accelerated Branch and Bound algorithm (ABB), 157–158 ADAS, Inside and Solutions, 297 Advanced Process Combinatorics, Inc., 310 AEA Technology, 4 AIChE International Congress on Sustainability Science and Engineering (ICOSSE), 296, 309, 310 AIChE Journal, 310 algorithms: combinatorial, 8 curve-fitting methods search, 30 descent-based, 30 deterministic search solutions, 29–31 Fibonacci method search, 30 golden section method search, 30 gradient-based (local search), 28–29 HENs, 19 line search, 30 LPR models, 29 MSG, 38 Newton method search, 30 NLP models and simplex, 29 nonlinear unconstrained problems and search, 30 optimality conditions and global/ local search, 28–29 P-graphs and, 38, 158 PNS solutions and starting state of MSG, 192 primal, 31 process synthesis and heuristic, 13– 14 PTA, 56–60 SSG, 38

American Process Inc., 301, 305 Analysis of Variance (ANOVA), 43 ant colony optimization stochastic search method, 32 AO Sodrugestvo-T, 300, 303 Applied Thermal Engineering, 301, 307 aqueous streams, 23 arcs, 161 Artie McFerrin Department of Chemical Engineering, Texas A&M, 297, 301, 305 ASPEN, 202–203 AspenTech, 297, 307, 310 audits of energy, 5, 6 availability: optimization, reliability and, 186–190 P-graph solution for energy system, 186 PI and integrating maintainability, reliability and, 144–146 azeotropic distillation systems: maximal/optimal structure for base-case synthesis, 175 optimal process synthesis and, 173–176 P-graph representing structure of, 176 process steps incorporated into base case, 174 residue of curve map, 175

B Balanced Composite Curves (BCCs), 15, 68–69 heat recovery targets, utility placement and, 239 balancing technology, 7 barrier methods, 31 BAT. See best available techniques

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Index batch processes: increase in value of objective function, 160 infeasible solution generated by MILP approach, 160 number produced of each product, 280 optimal solution generated by S-graph, 161 process optimization frameworks and scheduling of, 159–163 S-graphs and, 160–161 BCCs. See Balanced Composite Curves best available techniques (BAT), water and, 107–108 bilinear optimization problem, 27 binary variable, 27 biofuels, 3 biorefineries, green: flowsheet of, 173 solution network for workflow synthesis problem, 172 synthesis of, 171–173 BIS (Department for Business, Innovation and Skills), 297 black box (steady-state model), 23–24 blue water, virtual, 109 bounding function, role in solving MIP, 32 branch and bound approach, for solving discrete problems, 31 budget-income-time pinch analysis: CCs for project budget and income, 132 PI and, 131–133 project budget and income with time, 132

C Canadian Society for Chemical Engineering, 11 CAPE (Computer Aided Process Engineering), 11 capital costs: data extraction with operating and, 290–292 heat transfer area, total cost targeting and, 69–70 carbon dioxide emissions (CO2), 138– 139 costs related to, 2 FC-based systems and, 9 FCs, gas turbines and, 4 carbon footprint (CFP), 20 conclusions and further information, 319–320

carbon footprint (CFP) (Cont.): defined, 2 PI application, 13 and product life-cycle assessment, 2–3 carbon neutrality studies, 2 Carbon Trust, 5 case studies/examples: de-bottlenecking HI crude-oil distillation system, 256–262 energy efficiency in other food/ drink industries, 268–271 energy recovery from FCC unit, 253–256 heat pinch technology, 219–226 heat/power integration in buildings/building complexes, 275–277 industrial applications and, 253–280 industrial utility systems synthesis, 271–275 minimizing water/wastewater in citrus juice plant, 262–268 optimal design of supply chain, 277–279 scheduling large-scale paint production system, 279–280 total sites, 226–233 utility placement, 238–246 water pinch technology, 247–252 CCs. See Composite Curves Center for Engineering and Sustainable Development Research, De La Salle University, 297 Centre for Advanced Process Decision-Making, Carnegie Mellon University, 297 Centre for Process Integration, University of Manchester, 8, 13, 297, 301, 305, 307 Centre for Process Integration and Intensification, European Community Project, 298, 302, 305, 307 Centre for Process Systems Engineering, Imperial College London, 298, 310 Centre for Technology Transfer in the Process Industries, Bucharest, 298 CFP. See carbon footprint Charles Parsons Institute, University of Limerick, 298, 302, 305, 308 CHEMCAD, 205–206 Chemical Engineering, Chemical Equipment Design and Automation (CHISA), 296

Index Chemical Engineering and Processing, 307, 310 Chemical Engineering Science, 307, 310 Chemical Engineering Transactions, 297, 307, 310 Chemical Process Engineering Research Institute (CPERI), 302 CHISA. See Chemical Engineering, Chemical Equipment Design and Automation Chiyoda Corporation, Energy Frontier Business Development Office, 298 CHP. See Combined Heat and Power (CHP) systems CLIMA Congress, 296 CO2. See carbon dioxide emissions cogeneration, 4–5 in advanced gas turbines/FCs, 4 application of PI/HI method to, 12–13 in oil refineries, 4–5 Cold Composite Curve, 15 combinatorial algorithms, 8 combined analysis: conferences, 306 journals, 307 projects, 308–309 service providers, 307–308 Combined Heat and Power (CHP) systems, 4, 7 compact heat exchangers, 4 Composite Curves (CCs): BCCs, 15, 68–69 cold, 15 data precision and, 286 EGCCs and, 270 FCC process with, 254 GCCs and, 60–64, 79, 221, 227, 229, 232, 235, 246, 270 heat recovery and constructing total site, 99 heat recovery for multiple streams and, 51–54 hot, 15, 52 materials reuse-recycle and supply chain, 138 regional resource management, 142 shifted, 63 utility placement and, 245 water minimization, WATER and limiting, 266 water pinch technology and limiting, 249 Computer Aided Chemical Engineering, 307 Computer Aided Process Engineering (CAPE), 11

Computer-Aided Systems Laboratory, Princeton University, 310 Computers & Chemical Engineering, 310 Conceptual Design of Chemical Processes (Douglas), 315 conceptual modeling: data extraction about operating units, 34 network/topology data identification, 34–35 conclusions: better utilization of low-grade heat, 319 books and key articles, 313–315 development trends, 316–320 energy planning, CFP and, 319–320 hybrid energy conversion systems, 317 integration of renewables and waste, 317–319 lecture notes and online teaching resources, 315 maintenance scheduling, maintainability and reliability, 316–317 optimization and optimal design of industrial processes, 315 PI and, 313–315 top-level analysis, 316 Conference on Process Integration, Modeling and Optimisation for Energy Saving and Pollution Reduction, 11 conferences, 11 combined analysis, 306 general information sources, 295–296 HI, 301 mass integration, 304 optimization for sustainable industry, 309–310 continuous variables, 26 convex optimization problem, 27 cooling: demand and data extraction, 50 HI parameter values for heating and, 183 water, 51 COWI A/S, 298 CPERI. See Chemical Process Engineering Research Institute CPLEX code, 35 crude-oil distillation system: changes in heat transfer area due to retrofit, 260 de-bottlenecking heat-integrated, 256–262

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Index crude-oil distillation system (Cont.): flowsheet of, 257 initial HENs for, 259 modified HENs for, 261 pinch analysis results for operating points of preheating phases, 258 curve-fitting methods search algorithms, 30 cutting planes, for solving discrete problems, 31 Czech Society of Chemical Engineering, 11

D Dansk Energi Analyse A/S, 297 data extraction: avoiding pitfalls, 283–292 calculating heat loads and temperatures of extracted streams, 289–290 changes in specific heat capacities, 286–287 conceptual modeling, 34, 40 estimating capital and operating costs, 290–292 example process flowsheet, 49 extracting at effective temperatures and, 289 extracting utilities and, 288 extraction of cold stream and, 288 from flowsheet heat loads, 290 forced and prohibited matches, 289 generating utilities and, 288–289 heat losses and, 288 heating and cooling demands, 50 HI and, 48 integrated placement of processing units and, 234–238 keeping streams separate when necessary, 289 plus-minus principle with soft, 291 precision, 285–286 rules /guidelines, 287–289 soft data in plant/process flowsheet, 290 streams, 284–285, 289–290 data validation technology, 7 decarbonization, 142–143 decision variables, 25 DEFRA (Department for Environment, Food and Rural Affairs), 298 Department of Chemical and Biochemical Engineering, University of Denmark, 302

Department of Chemical and Environmental Engineering, University of Nottingham Malaysia, 298 Department of Chemical and Process Engineering, Rzeszow University of Technology, 302 Department of Chemical Engineering: Auburn University, 297 MIT, 298 University of Maribor, 298 University of Massachusetts, 308 University of Monash, 302, 305 University of Pretoria, 298 Department of Computer Science and Systems Technology, University of Pannonia, 299, 310 Department of Energy, U.S., 300 Department of Energy and Climate Change, U.K., 299 Department of Energy and Environment, Chalmers University, 299, 302 dependent variables (in process optimization), 25 descent-based algorithms, 30 detailed audit, 6 deterministic search algorithm solutions: constrained nonlinear p roblems and, 31 solving continuous LPR problems and, 29 solving continuous NLP problems and, 29–31 solving discrete problems and, 31–32 unconstrained nonlinear problems, 30 diagrams: CCs, hydrogen networks and hydrogn surplus, 124 FCC grid, 255 heat pinch technology and calculated grid, 222 HENs and grid, 83, 84 IT-domain/UML, 24 materials resue-recycle and interval flow rate, 136 MRPD, 116–117 onion, 48 utility placement and preliminary grid, 241 water pinch technology and minimum water flow rate, 250 distillation processes: appropriate placement against GCCs, 79

Index distillation processes (Cont.): distillation column and, 78 extended pinch technology and, 77–80 heat pump placement across utility pinch, 77 refrigeration systems and, 77 dividing-wall distillation technology, 4 Dubrovnik Conference on Sustainable Development of Energy, Water and Environment Systems, 296, 301

E EC. See European Community ECCE. See European Congress of Chemical Engineering Ecological Modelling, 307 EEBPp/U.K. See Energy Efficiency Best Practice Programme EGCC. See exergy grand composite curve emergy-pinch analysis, 126–129, 130–131 EMINENT 2, 214, 303 emissions/effluents: CO2 emissions, 138–139 FCCC system boundary and processing steps, 184 flowsheet and P-graph of FCCC system, 184 materials, streams and, 185 minimizing, 183–186 types of, 23 energy: audits of, 5, 6 low-temperature, 143–144 recovery case study, 253–256 renewable, 2, 3–4, 216–218, 317–319 superstructure for lowtemperature, 143 targets, 51–54 Energy, 301, 307 energy efficiency: basic pinch technology and, 50–69 Carbon Trust recommendations, 5–6 CFP and, 319–320 defined, 3 EGCC for meat-processing plant and, 270 extended pinch technology and, 69–81 food/drink industries and, 268–271 heat recovery pinch and, 54–56

energy efficiency (Cont.): HENs synthesis and, 81–96 importance of optimization, 2 improvement studies, 11 PI basics and, 47–50 PI for improving, 45–104 Pinch Technology and, 3, 14, 50–69 proposed utility system matched to process GCCs, 270 technology examples, 4 total site energy integration and, 96–104 U.K residential data (1971), 8 Energy Efficiency Best Practice Programme (EEBPp/U.K.), 6 Energy Information Administration, USA, 299 Energy Research Group, University of Waikato, 299, 302 Energy Science and Engineering, Indian Institute of Technology, 299, 302 energy systems: flowsheet and hP-graph, 177 optimal retrofit design and, 177–179 optimization and synthesis of, 176–179 simple HI and, 176–177 Environmental Protection Agency (EPA), U.S., 300, 303, 311 EPA. See Environmental Protection Agency equation construction, 35–37 ESCAPE. See European Symposium on Computer Aided Process Engineering EUBIONET 3, 304 Europe Energy Efficiency Conference, 296 European Community (EC), 8 European Congress of Chemical Engineering (ECCE), 296 European Federation of Chemical Engineering Working Party, 11 European Integrated Pollution Prevention and Control Bureau, 299 European Symposium on Computer Aided Process Engineering, 295, 310 European Symposium on Computer Aided Process Engineering (ESCAPE), 11 evaluation tree, of MILP, 31–32 EVECO Brno, 299, 302 exergy grand composite curve (EGCC), 270

349

350

Index

F Faculty of Technology, Lappeenranta University of Technology, 302 FCC. See Fluid Catalytic Cracking unit FCCC. See Fuel-Cell Combined Cycle (FCCC) subsystems FCs. See fuel cells Fibonacci method search algorithm, 30 flow-rate targeting: MRPD and, 116–117 MRPD for pure/impure fresh resource, 117 flowsheeting simulation packages: ASPEN, 202–203 CHEMCAD, 205–206 gPROMS, 204 HYSYS and UniSim Design, 203 PRO/II, 206 software tools, 202–206 flowsheeting simulation tools, 39, 40 optimization technology and, 7 flue gases, 23 Fluid Catalytic Cracking unit (FCC): CCs and, 254 energy recovery case studies/ examples, 253–256 grid diagram of chosen retrofit option, 255 process example, 21 FOB (Free On Board) cost estimate method, 16 food industry, HI application, 13 footprints: carbon, 2–3, 13, 20, 319–320 water, 108–111, 320 Fraunhofer Institute for Environmental, Safety and Energy Technology (UMSICHT), 299 Frontline Systems, 209 fruit juice case study, 111–112, 117–118, 119 fuel cells (FCs): CO2 emissions and, 4, 9 cogeneration in advanced gas turbines and, 4 Fuel-Cell Combined Cycle (FCCC) subsystems, 8–9 emission/effluents and, 184

G GA technique application (stochastic search method), 32 GAMS, 35, 206–207

gas turbines, advanced, 4 gaseous waster streams, 23 GCCs. See Grand Composite Curves general information sources. See information sources, general genetic programming stochastic search method, 32, 33 Global Footprint Network, 299 global optimality, 28–29 global warming, 11 golden section method search algorithm, 30 good housekeeping approach, water/ wastewater, 5 Gover transformation reformulation technique, 42 gPROMS, 204 gradient-based (local search) algorithms, 28–29 Grand Composite Curves (GCCs): appropriate placement of distillation against, 79 construction and multiple utilities targeting, 63 heat pinch technology and, 221 processing units and, 235 proposed utility system matched to, 270 relation between SCCs and, 64 threshold problems and, 60–61 total sites for process A, 227, 229, 232 total sites for process B, 229, 232 utility placement and, 246 utility placements and, 61–62 graph-theoretical approach, 35 gray box (steady-state model), 23–24 green biorefineries, 171–173 green water, virtual, 108 greenhouse gas emission: CFP and, 2 reduction methods, 3–4, 5, 11 grey water, virtual, 109

H heat: better utilization of low-grade, 319 integration and data extraction, 48 steam, 50–51 heat engines: appropriate placement of, 72 configuration, 71 HI of energy-intensive processes and, 71–72 integrating steam turbine above pinch, 72

Index Heat Exchanger Networks (HENs), 12–13 achievable target calculations, 39 algorithms, 19 CCs and, 15 compact, 4 completed design, 89 completing design, 87–92 conventional flowsheet, 82 cost estimation and, 16 data extraction design considerations, 40 design above pinch, 88 design above process pinch and utility placement, 242 design below pinch, 88 design below process pinch and utility placement, 241 design procedure, 83–87 of the FCC process (example), 21 feasible heat exchanger match above pinch, 86 general process flowsheet to represent, 82 grid diagram and implications of pinch, 84 grid diagrams for, 83 heat recovery and, 45–47 Heat Recovery pinch concept and, 14–15 hot/cold streams with, 89 hybrid approach, 95–96 implementing matches with, 47 infeasible heat exchanger match above pinch, 86 key features of resulting networks, 96 mass balances/problems, 36 matches, 46–47 MER for, 39 multistream, 4 pinch design method, 81–93 pinch design principle and, 85 retrofitting of, 16–17, 21 spaghetti-type topology (of heat transfer), 15 splitting above pinch and, 89 splitting and trivial tick-off, 91 splitting below pinch and, 90 splitting to enable CP values for essential matches and, 91 superstructure approach, 93–95 supertargeting of, 15–16, 17 synthesis, 81–96 synthesis methods, 14, 19, 38–40 tick-off heuristic and, 87

Heat Integration (HI), 7–8 building complexes, power and, 275–277 conferences, 301 crude-oil distillation system and de-bottlenecking with, 256– 262 distillation processes and, 77–80 energy-intensive processes and, 71–80 Gantt chart of optimal solution, 183 globally optimal schedule for case study, 181 heat engines and, 71–72 heat pumps and, 72–77 HENs and, 12–13 IEA definition, 12 journals, 301 methodology dissemination, 113 parameter values for heating/ cooling, 183 power systems and, 142–144 process CCs for hospital complex, 276 process stream data of hospital complex, 276 production schedules, 180–183 projects, 303–304 recipes for products, 182 scheduling data for case study, 180 service providers, 301–303 S-graph representing recipe for case study, 181, 182 Heat Integration tools: HEAT-int, 195 HEXTRAN, 199–200 SITE-int, 198 software and, 195–201 spreadsheet-based, 200–201 SPRINT, 195 STAR, 195–198 SuperTarget, 200 WORK, 198–199 heat pinch technology: calculated grid diagram and, 222 calculated MER heat cascade, 221 case studies, 219–226 exchangers violating pinch, 224 existing HENs and, 220 first problem, 219–224 GCCs, 221 load-shirt path identified, 222 minimum allowed temperature difference, 225 optimal HENs and, 226 process stream data, 224

351

352

Index heat pinch technology (Cont.): second problem, 224–226 utility requirements and cost, 225 heat pumps, 7 configuration, 73 HI of energy-intensive processes and, 72–77 placement against heat recovery problem, 74 procedure for sizing, 74 sizing example, 75–76 heat recovery: constructing hot CCs and, 52 constructing total site CCs and, 99 evaluation of multiple streams, 51–54 heat exchange and, 45–47 heat exchange matches and, 46–47 between hot/cold stream, 51 implementing matches with, 47 limits for process, 54 problem and partitioning, 55–56 problem identification and PI basics, 48–50 via steam systems, 99–100 targeting, 100 thermodynamic limits on, 51 variation of targets with, 53 heat recovery pinch: energy efficiency and, 54–56 HENs and, 14–15 limits for process heat recovery set by, 54 trade-off between investment and energy costs with, 54 heat transfer: area, capital cost and total cost targeting, 69–70 enhancement and pressure drop, 146–148 Heat Transfer Engineering, 301 HEAT-int, 195 Hebling Technik, 308 HENS. See Heat Exchanger Networks HEXTRAN, 199–200 HI. See Heat Integration high-temperature FCs (MCFC/SOFC), 4 hill climbing stochastic search method, 32 Honeywell, Canada, 311 hospital complex example, 21 Hot Composite Curve, 15, 52 hot oil utilities, 66 Housing and Urban Development (HUD) Department, U.S., 3

HUD. See Housing and Urban Development Hungarian Chemical Society, 11 hybrids: approach, 95–96 energy conversion systems, 317 hydrogen networks CCs and hydrogen surplus diagram with, 124 PI and, 123–125 HYSYS/UniSim Design, 203

I ICheaP. See Italian Conference on Chemical and Process Engineering ICOSSE. See AlChE International Congress on Sustainability Science and Engineering IEA. See International Energy Agency ILOG ODM, 209–210 Industrial & Engineering Chemistry Research, 310 industrial applications: case studies and, 253–280 de-bottlenecking heat-integrated crude-oil distillation system, 256–262 energy efficiency in food/drink industries, 268–271 energy recovery from FCC unit, 253–256 heat/power integration buildings and building complexes, 275–277 minimizing water/wastewater in citrus juice plant, 262–268 optimal design of supply chain, 277–279 scheduling large-scale paint production system, 279–280 synthesis of industrial utility systems, 271–275 information hiding, 39 information sources, general: combined analysis, 306–309 conferences, 11, 295–296, 301, 304, 306, 309–310 further reading and, 295–311 general, 295–301 HI, 301–304 journals, 297, 302, 304–305, 307, 310 mass integration, 304–306 optimization for sustainable industry, 309–311

Index information sources, general (Cont.): projects, 301, 303–304, 306, 308–309, 311 service providers, 297–301, 302–303, 305–306, 307–308, 310–311 Institute for Scientific Research, University of Guanajuato, 299 Institute of Process and Environmental Engineering, Brno University, 299, 302 integer programming (IP) model, 25, 27 integer variables (in process optimization), 26, 27 International Energy Agency (IEA), 300 energy monitoring techniques and, 3 Heat Energy definition of, 12 IP. See integer programming Italian Association of Chemical Engineering, 11 Italian Conference on Chemical and Process Engineering (ICheaP), 296, 301, 306

J Journal of Clean Technologies and Environmental Policy, 304, 307 Journal of Cleaner Production, 297, 305, 307 Journal of the Chinese Institute of Chemical Engineers, 310 Journal of Universal Computer Science, 310 journals: combined analysis, 307 general information sources, 297 HI, 301 mass integration, 304–305 optimization for sustainable industry, 310

K KBC Energy Services, 300, 303, 305 key performance indicators (KPIs), 7 KKT (Karush-Kuhn-Tucker) optimality conditions, 28

L Laboratory for Analysis and Synthesis of Chemical Systems, Institut de Chimie-Bâtiment B6, 303

Laboratory for Industrial Energy Systems, Ecole Polytechnique Federale de Lausanne, 300, 303, 311 Lagrange multipliers, 28 laws, second thermodynamic, 51 legislation, water, 106–107 Lehrstuhl für Technische Chemie A, 300 life-cycle assessment, 2–3, 20 LINDO, 208–209 line search algorithm, 30 linear optimization problem, 27 linear programming (LPR) models, 25 absence of integer variables and, 27 branch and bound method solution, 31–32 convex, 28 deterministic algorithm solutions, 29 equation construction, 35, 36 Simplex Method (algorithm) solution, 29 Linnhoff, Bodo, 3, 13, 283, 294, 313–314 local optimality, 28 Loss Prevention and Safety Promotion in the Process Industries, 304 LPR. See linear programming models

M maintainability: maintenance scheduling, reliability and, 316–317 PI, integrating reliability, availability and, 144–146 mass balances, 36–37 mass integration: conferences, 304 design for low-temperature energy systems, 144 flow-rate targeting with MRPD, 116–117 general information sources, 304–306 journals, 304–305 MRPD applied to fruit juice case study, 117–118 new process design methodology, 145 projects, 306 service providers, 305–306 software, 201–202 summary, 122 water, minimizing use and maximizing reuse, 106–113

353

354

Index mass integration (Cont.): water integration and, 105–106 water minimization via mathematical optimization, 118–122 water pinch analysis introduction, 113–116 material recovery pinch diagram (MRPD): flow-rate targeting and, 116–117 fruit juice production, limiting water data and, 117 MRPD for pure/impure fresh resource, 117 materials reuse-recycle: construction of interval flow rate diagram, 136 material balance in aggregate planning, 137 property pinch analysis and, 133–136 supply chain CCs and, 138 mathematical modeling suites: MATLAB, 210–211 MATLAB alternatives, 211 software tools, 210–211 mathematical optimization fruit juice production, MRPD and network design, 119 illustrative example of brewery plant, 120–122 introduction to, 118–119 water minimization via, 118–122 Mathematical Programming (MPR) approach, 8, 14 model building/optimization and, 24 model nonlinearity and, 41–42 Network Pinch and, 17 network-related information transformation, 35 PI and, 14 process optimization frameworks and, 151–153 process synthesis major steps and, 153 superstructure formulation, 35–36, 38 tools for designing chemical processes, 20 MATLAB, 24, 29, 210–211 Maximal Energy Recovery (MER), 39 Maximal Structure Generation (MSG) algorithm, 38, 157–158, 192 MCFCs. See molten-carbonate fuel cells

Mechanical Engineering Faculty, Paderborn University, 300 MER. See Maximal Energy Recovery MILP. See mixed integer linear program MINLP. See mixed integer nonlinear program MIPSYN, 207–208 mistakes. See pitfalls mixed integer linear program (MILP), 25, 29, 160. See also successive mixed integer linear program convexity case-by-case evaluation, 28 described, 27 deterministic methods for solving, 31–32 global optimality and, 29 mass balances/problems, 36 nodes/evaluation tree of, 31–32 mixed integer nonlinear program (MINLP), 25, 27 deterministic methods for solving, 31–32 mass balances/problems, 36 model building and optimization, 24–25 components, 24–25 examples, 24 IT-domain diagrams/UML diagrams, 24 model creation, 33–43 conceptual modeling, 34–35 equation construction, 35–37 evaluating adequacy and precision, 42–43 graph-theoretical approach, 35 handling model nonlinearity, 41 handling process complexity, 38–40 mass balances, 36–37 objective function choice, 37–38 object-oriented modeling, 38–39 P-graph framework, 35 process insight application, 40–41 Modelica modeling language, 24, 211–212 molten-carbonate fuel cells (MCFCs), 4 MPR. See Mathematical Programming (MPR) approach MRPD. See material recovery pinch diagram MSG algorithm. See Maximal Structure Generation algorithm multiple utilities targeting: construction of GCCs and, 63

Index multiple utilities targeting (Cont.): pinch technology and, 61–69 utility placement options, 63–69 utility placements, GCCs and, 61–62 multistream heat exchangers, 4

N network evolution: loops, paths and, 93 splitting and advanced tick-off with, 92 splitting procedure above pinch, 92 network optimization, 8 Network Pinch method, 16–17, 21 network/topology data identification, 34–35 Newton method search algorithm, 30 NLP. See nonlinear programming (NLP) models nodes, of MILP, 31–32 nonisothermal stream mixing, 287 nonisothermal utilities, 65–66 Nonlinear and Mixed-Integer Optimization: Fundamentals and Applications (Floudas), 315 nonlinear programming (NLP) models: absence of integer variables and, 27 convexity case-by-case evaluation, 28 equation construction, 35 mass balances/problems, 36 penalty methods for solving constrained, 31 simplex algorithm for problem-solving, 29 numerical targeting, 56–60

O objective function, 25 object-oriented modeling, 38–39 oil crises (1973–1974, 1979), 14 onion diagram, 48 open-source DWSIM chemical process simulator, 24 operating costs, 290–292 optimal process synthesis: azeotropic distillation systems and, 173–176 classification of optimization methods, 167 heterogeneous flowsheets and, 169– 171 optimization and, 167–176 reaction network synthesis and, 167–169

optimal process synthesis (Cont.): steps for composition of maximal structure, 169 synthesis of green biorefineries and, 171–173 optimal workflow structures: P-graph, 171 plausible activities for, 170 synthesis of heterogeneous flowsheets and, 169–171 optimality conditions: global search algorithms, 28–29 local search algorithms, 28 optimality problems, stochastic search methods for solving, 32–33 optimization: availability, reliability and, 186–190 combined PI and, 165–190 emissions/effluents minimized and, 183–186 methods with optimal process synthesis, 167 network, 8 optimal design of industrial processes and, 315 optimal process synthesis and, 167–176 optimal scheduling for throughput, profit, security and, 179–183 optimal synthesis of energy systems and, 176–179 process synthesis and role of, 165–166 summary, 190 tools for efficient implementation of PI, 166–167 water minimization via mathematical, 118–122 optimization, sustainable industry: conferences, 309–310 journals, 310 projects, 311 service providers, 310–311 optimization packages, general-purpose: Frontline Systems, 209 GAMS, 35, 206–207 ILOG ODM, 209–210 LINDO, 208–209 MIPSYN, 207–208 software tools, 206–210 optimization technology: application, 9 flowsheeting simulation tools, 7 HENs retrofit, 16–17

355

356

Index optimization technology (Cont.): PI integration attempts, 13 sustainable industry and, 309–311 OSL code, 35 oxygen pinch analysis, 125–126 oxygen-water pinch analysis, 128–129

P paint production system, scheduling, 279–280 parity plots, 43 Parliamentary Office for Science and Technology, U.K., 2 penalty methods, for solving constrained NLP, 31 PEPNET, 304 performance targets, 48 P-graphs, 8–9 algorithms and inputs/outputs from, 158 availability and solution for energy system, 186 azeotropic distillation systems structure and, 176 emissions/effluents flowsheet and, 184 mathematical engine, 157–158 model building/optimization and, 24, 35 MSG/SSG algorithms, 38 optimal retrofit design, maximal structure and, 179 optimal workflow structures, 171 process representation via, 154–155 process structure of operating units and, 155 process structure violating axioms and, 157 reduction in search space, combinatorial axioms and, 157 significance for structural process optimization, 155–157 structural process optimization and, 153–158 symbols of process elements and, 154 PI. See Process Integration (PI) Pinch Analysis: benefits of using, 40–41 data extraction and, 283–284 for HI, 41 PI example, 21 pinch design method: completing designs and, 87–92 design procedure and, 83–87

pinch design method (Cont.): HENs representation and, 81–83 network evolution and, 92–93 Pinch Express, 283 Pinch Technology: energy efficiency and basic, 3, 14, 50–69 energy efficiency and extended, 69–81 heat recovery pinch and, 54–56 heat transfer area, capital cost, total cost targeting and, 69–70 HI of energy-intensive processes and, 71–80 multiple utilities targeting and, 61–69 numerical targeting, PTA and, 56–60 process modifications and, 80–81 setting energy targets, 51–54 threshold problems and, 60–61 Pinch Technology (Linnhoff and Vredeveld), 3 pitfalls, 281–282 data extraction, 283–292 integration of renewables, fluctuating demand and supply, 292 interpreting results, 293 making results happen, 293–294 steady-state and dynamic performance, 292–293 PNS solutions: graph-based process optimization tools and, 191–193 starting state of MSG algorithm, 192 power: cogeneration, 101–102 integration, building complexes and HI, 275–277 water, 3 wind, 3 PRES. See Process Integration, Modelling and Optimisation for Energy Saving and Pollution Reduction pressure drop, 146–148 primal algorithms, 31 Problem Table Algorithm (PTA): heat cascade for process data, 59 numerical targeting and, 56–60 process streams data, 58 temperature shifting to ensure feasible heat transfer and, 57

Index process design: onion diagram and, 48 PI, energy efficiency and, 47–48 Process Design Center, Netherlands, 303 Process Integration, Modelling and Optimisation for Energy Saving and Pollution Reduction (PRES), 295, 301, 306 Process Integration (PI): application of, 7, 9 audit procedure, 6 avoiding pitfalls, 281–294 benefits of, 18–20 data extraction, steps of, 34 defined/described, 12 examples, 20–22 further applications of, 123–150 HI component, 7–8 history and development of, 12–14 improving energy efficiency and, 45–104 MPR approach to, 14 needs for, 11–12 Network Pinch, 16–17 optimization and, 165–190 optimization integration attempts, 13–14 role in industrial sustainability, 20 targeting heat recovery and, 14–15 thermodynamic roots of, 14–15 Process Integration (PI), energy efficiency and: basic pinch technology, 50–69 basics, 47–50 extended pinch technology, 69–81 heat recovery problem identification and, 48–50 HENs synthesis, 81–96 HI and, 47 hierarchy of process design and, 47–48 introduction to heat exchange and recovery, 45–47 performance targets and, 48 total site energy integration, 96–104 Process Integration (PI), further applications of: budget-income-time pinch analysis, 131–133 combined analysis II, 131–142 decarbonization, 142–143 design and management of hydrogen networks, 123–125 energy-water, oxygen-water, pinch-emergy, 126–131

Process Integration (PI), further applications of (Cont.): heat-integrated power systems and, 142–144 integrating reliability, availability and maintainability, 144–146 local integrated energy sectors and extended total sites, 148–149 low-temperature energy, 143–144 materials reuse-recycle and property pinch analysis, 133–136 oxygen pinch analysis, 125–126 pinch analysis of supply chains, 136–138 pinch used to target CO2 emissions, 138–139 pressure drop and heat transfer enhancement in, 146–148 regional resource management, 139–142 summary, 149–150 Process Integration Ltd., 300, 303, 305, 308, 311 process modifications: hot and cold streams with, 81 plus-minus principle and, 80 process network model construction, 36–37 process optimization, 23–43 classes of problems, 26–28 conditions for optimality, 28–29 continuous/integer variables and, 26 creating models, 33–43 decision/dependent variables and, 25 defined, 25 deterministic algorithm solutions, 29–31 deterministic methods for solving discrete problems, 31–32 generic optimization problem, 26t integer/binary variables and, 27 mathematical problem formulation, 25–26 model building and, 24–25 objective function component, 25 stochastic search methods, 32–33 process optimization frameworks: mathematical programming, classical approach and, 151–153 scheduling of batch processes and, 159–163 structural process optimization, P-graphs, 153–158

357

358

Index process optimization tools, graph-based: PNS solutions, 191–193 S-Graph Studio, 193–195 software tools, 191–195 Process Pinch, 21, 22 process synthesis: heuristic/algorithmic methods of, 13–14 major steps and mathematical programming, 153 optimization’s role in, 165–166 P-graph synthesis, 8–9 process system engineering, 11 A Process Integration Primer (Gunderson), 295 processing units: CCs for process in problem 5, 234 data extraction and integrated placement of, 234–238 GCCs for process in problem 5, 235 process flowsheet for base-case design and, 234 stream data for pinch analysis and, 237 PRO/II, 206 projects: combined analysis, 308–309 general information sources, 301 HI, 303–304 mass integration, 306 optimization for sustainable industry, 311 property pinch analysis, materials reuse-recycle and, 133–136 PTA. See Problem Table Algorithm

R recipes, 161 HI, 181–182 S-graph example, 162 S-graph representing case study, 181 reconciliation technology, 7 refrigeration, 7 levels, 67–68 systems and distillation processes, 77 utility systems and, 271 WORK and composition options/ ideal profiles with, 199 reliability: maintenance scheduling, maintainability and, 316–317 optimization, availability and, 186–190

reliability (Cont.): PI and integrating availability, maintainability and, 144–146 renewable energy: carbon neutrality and, 2 energy system sustainability from, 3–4 energy systems and integrating, 216–218 integration of waste and, 317–319 software for analyzing integration of, 216 Renewable Energy, 301, 307 residual plots, 43 resource management, regional: CCs and, 139–141, 142 flowchart of algorithm for, 140 PI and, 139–142 regional energy supply-deficit curves and, 141 surplus-deficit curves, 141 Resources, Conservation & Recycling, 297, 305, 307 retrofit design, optimal: characteristics, operating unit costs and, 178 energy systems and, 177–179 flowsheet for considering absorption, 179 P-graph of maximal structure, 179 revenue, maximizing, 179–180

S SA. See simulated annealing SCCs. See Shifted Composite Curves scheduling: batch processes and process optimization frameworks, 159–163 frameworks, suitability, limitations and S-graphs, 159–161 graph of solution minimizing makespan, 280 large-scale paint production system, 279–280 number of batches produced of each product, 280 optimization, throughput, security and optimal, 179–183 reliability, maintainability and maintenance, 316–317 S-graphs and framework for, 161–163 School of Chemical and Environmental Engineering, University of Nottingham Malaysia, 305, 308

Index School of Chemical Engineering, Purdue University, 311 Scilab computational package, 24 Scottish Environment Protection Agency (SEPA), 300 screening and scoping audits, 5–6 search algorithms, for nonlinear unconstrained problems, 30 second law of thermodynamics, 14–15 segmentation, 286–287 SEMPRA ENERGY, 3 SEPA. See Scottish Environment Protection Agency service providers: combined analysis, 307–308 general information sources, 297–300 HI, 301–303 mass integration, 305–306 optimization for sustainable industry, 311 S-Graph Studio, 193–194 S-graphs: batch processes and, 159–163 example recipe, 162 framework for scheduling, 161–163 HI and recipe for case study with, 181, 182 recipe for two batches, 162 scheduling frameworks, suitability and limitations, 159–161 solution for recipe under NIS policy, 162 Shifted Composite Curves (SCCs), 63 relation between GCCs and, 64 simple heat integration, 176–177 simplex method algorithm for LPR problems, 29 simulated annealing (SA) stochastic search method, 32, 33 simulation tools, 39 for process industry, 24 SITE-int, 198 SMILP. See successive mixed integer linear program SOFCs, 4 software tools: balancing/flowsheeting simulation for energy-saving analysis, 215 emerging trends, 212–215 flowsheeting simulation packages, 202–206 general-purpose optimization packages, 206–210 graph-based process optimization tools, 191–195

software tools (Cont.): HI tools, 195–201 integrating renewable energy into other energy systems, 216–218 mathematical modeling suites, 210–211 Modelica, 24, 211–212 other, 211–218 overview of available, 191 WATER, mass integration software, 201–202, 266 Solution Structures Generation algorithm (SSG), 38, 157–158 specifications, 25 spreadsheet-based tools, 200, 201 SPRINT: HI tools and, 195, 286 software interface, 196 SSG algorithm. See Solution Structures Generation algorithm STAR, 286 graphical user interface, 196 HI tools and, 195–198 steady-state models, 23–24 steam: heating with, 50–51 system and heat recovery, 99–100 stochastic methods: error minimization tools and, 43 optimization problems and, 32–33 streams: aqueous, 23 CCs and heat recovery for multiple, 51–54 data extraction and, 284–285, 289–290 emissions/effluents, materials and, 185 heat exchangers and multi, 4 heat recovery between hot and cold, 51 structural process optimization: mathematical programming and, 153–158 MSG, SSG, ABB and, 157–158 P-graph symbols of process elements and, 154 P-graphs and process structure of operating units, 155 P-graphs and process structures violating axioms, 157 P-graph’s mathematical engine and, 157–158 P-graph’s significance for, 155–157 process representation via P-graphs, 154–155 reduction in search space, combinatorial axioms and, 157

359

360

Index successive mixed integer linear program (SMILP), 42 sunflower oil production, 21 superstructure approach: HENs synthesis and, 93–95 loop and path in heat exchanger network, 93 spaghetti fragment and, 94 SuperTarget, 200, 283 supertargeting, 15–16, 17, 70 supply chain: activities in optimal, second/thirdbest business processes, 279 case study, optimal design of, 277–279 CCs and materials reuse-recycle, 138 cost of activities in case study, 278 potential activities in case study, 277 Systematic Methods of Chemical Process Design (Biegler et al.), 315

T Tabu search, 32 TAPPI EPE (Engineering, Pulping and Environmental Conference), 296 targeting procedures, 39 targets: energy, 51–54 variation of heat recovery, 53 Thermal Energy, Norwegian University of Science and Technology, 300, 303 thermodynamics: limits on heat recovery, 51 roots, 14–15 second law, 51 threshold: HENs design cases, 60 low and high, 61 problems and GCCs, 60–61 throughput: maximizing, 179–180 optimal scheduling for profit, security and, 179–183 tools: complexity management, 39 flowsheeting simulation packages, 202–206 HI, 195–201 mathematical modeling suites, 210–211 MPR and designing chemical processes, 20 optimization and efficient implementation of PI, 166–167

tools (Cont.): optimization packages, 206–210 PI efficient implementation, 166–167 PNS solutions and graph-based process optimization, 191–193 PNS solutions and S-Graph Studio, 193–195 process industry and simulation, 24, 39 software, 191–218 spreadsheet-based, 200, 201 stochastic methods and error minimization, 43 topology data identification, 34–35 Total Food, 296 total sites: case studies, 226–233 combined site heat sources for problem 3(c), 230 data extraction, 107 data for process A, 227 data for process B, 227 energy sector with heat and power, 148 first problem, 226–230 GCCs for process A, 227, 232 GCCs for process B, 229, 232 heat recovery targets for problem 4(a), 232 heat source and sink segments from GCCs for Process A, 229 heat source and sink segments from GCCs for Process B, 229 local integrated energy sectors and extended, 148–149 marginal steam prices for utility system with, 103 optimized utility system and, 103 for problem 4(b), 233 for problem 4(c), 233 problem table for process A, 228 problem table for process B, 228 profiles, 97–99 profiles for problem 3(c), 230 second problem, 231–233 stream data for process A, 231 stream data for process B, 231 total sites energy integration, 96 advanced total site optimization and analysis, 102–104 data extraction, 97 heat recovery pockets, construction of total sites profiles and, 98 heat recovery via steam system, 99–100 power cogeneration, 101–102 profiles, 97–99 schematic of industrial total site, 97

Index trends: conclusions, further information and development, 316–320 software tools and emerging, 212–215 tri-generation, 5

U UK Energy Research Centre, 300 UMSICHT. See Fraunhofer Institute for Environmental, Safety and Energy Technology Uni-Sim Design/HYSYS, 203 UniSim process modeling (Honeywell), 24 United Kingdom: Department of Energy and Climate Change, 299 Energy Efficiency Best Practice Programme, 6 Energy Research Centre, 300 heat exchange case study, 4 Parliamentary Office for Science and Technology, 2 residential energy consumption, 8 universities. See service providers; specific departments University College London Energy Institute, 300 A User Guide on Process Integration for the Efficient Use of Energy (Linnhoff et al.), 313 utility pinch, 64, 77 utility placement: appropriate, 246 available utilities and, 239 BCCs and heat recovery targets, 239 case studies, 238–246 CCs, 245 constraints for placing hot oil utilities and, 66 constructing GCCs for streams and, 63 exploiting GCCs pocket for utility substitution with, 68 first problem, 238–242 GCCs and, 246 generating steam below pinch, 67 heat cascade intervals and stream population, 244 HENs design above process pinch and, 242 HENs design below process pinch and, 241 options and multiple utilities targeting, 63–69

utility placement (Cont.): placing refrigeration levels for pure refrigerants, 68 preliminary grid diagram and, 241 problem table, 245 process streams and, 239, 243 process streams with missing data filled in, 240 properties of nonisothermal hot utilities and, 65 relation between GCCs and SCCs, 64 second problem, 243–246 using GCCs to target for single/ multiple steam levels and, 64 utilities available and, 243 utility systems: case study, synthesis of, 271–275 configuration data for total site, 272 operating scenarios for total site, 272 optimal, 274, 275 sensitivity analysis for reducing emissions, 274 superstructure of industrial, 273 temperature changed with refrigeration levels, 271 total site profiles and candidate steam pressure levels, 272

V variables: continuous/integer, 26 decision/dependent, 25 LPR and absence of integer, 27 vertical heat transfer, 15 Vredeveld, D. R., 3 VTT Technical Research Centre of Finland, 303, 306

W walk-through audit, 6 Warsaw University of Technology, 300, 303 waste, integration of renewables and, 317–319 Waste Management, 307 wastewater, 23 minimizing water usage and, 111–113 optimization of use approach, 5–6 overview of measures, 111–112 treatment, 112–113 WATER, 201–202, 266

361

362

Index water: BAT, 107–108 citrus juice plant, minimizing wastewater and, 262–268 common usage operations, 109 cooling, 51 footprint, 108–111, 320 integration, 105–106 legislation, 106–107 minimizing usage and waste, 111–113 minimizing use and maximizing reuse, 106–113 optimization of use approach, 5–6 pinch analysis introduction, 113–116 power, 3 quality, 128 Water Footprint Network, 306 water footprints, 320 virtual blue water, 109 virtual green water, 108 virtual grey water, 109 virtual water consumed while processing food industry products, 110 water minimization and, 111–112 water minimization: existing water network and, 264 fruit juice production, MRPD, network design and, 119 limiting CCs generated by WATER and, 266 via mathematical optimization, 118–122 summary of four design options, 267 superstructure for water/ regeneration reuse in brewery plant, 121 wastewater in citrus juice plant and, 262–268 water footprints and, 111–112 water network after pinch analysis and, 265 water reuse opportunities in brewery plant, 121

water networks: achievable target calculations, 39 mass exchange and, 17–18 water pinch analysis: limiting CCs and, 115 mass integration and, 113–116 problem data for water-using operations, 114 treatment system design and, 115 water pinch technology: case studies, 247–252 combined limiting water profiles, 248 connecting operations directly, 252 data for water-processing operation, 247 design grid for water system and, 251 design strategy, 250 diagram used to target minimum water flow rate, 250 first problem, 247–248 flowsheet representation of water system design, 252 limiting CCs and, 249 limiting water profiles for, 247 minimum wastewater targeting and, 248 removing water mains, connecting sources and sinks, 252 second problem, 249–252 streams connected with water mains and, 251 whiskey distillery, 22 wind power, 3 WORK: HI tools and, 198–199 refrigeration composition options and ideal profiles, 199 World Bioenergy, 296 World Congress of Chemical Engineering, 296 World Renewable Energy Congress: Innovation in Europe, 296 World Sustainable Energy Days, 296