After an overview of the fundamentals, limitations, and scope of reactive distillation, this book uses rigorous models for steady-state design and dynamic analysis of different types of reactive distillation columns and quantitatively compares the economics of reactive distillation columns with conventional multi-unit processes. It goes beyond traditional steady-state design that primarily considers the capital investment and energy costs when analyzing the control structure and the dynamic robustness of disturbances, and discusses how to maximize the economic and environmental benefits of reactive distillation technology.
Autorentext
WILLIAM L. LUYBEN, PHD, is Professor of Chemical Engineering at Lehigh University. In addition to forty years of teaching, Dr. Luyben spent nine years as an engineer with Exxon and DuPont. He has written nine books and more than 200 papers. He was the 2004 recipient of the Computing Practice Award from the CAST Division of the AIChE and was elected in 2005 to the Process Automation Hall of Fame.
CHENG-CHING YU, PHD, has spent sixteen years as a Professor at National Taiwan University of Science and Technology and four years at National Taiwan University. He has published over 100 technical papers in the areas of plant-wide process control, reactive distillation, control of microelectronic processes, and modeling of fuel cell systems.
Klappentext
Reactive distillation has economical and environmental advantages
Reactive distillation is a breakthrough process innovation with numerous applicationsin the petroleum and chemical industries. In systems with the appropriate chemistryand vapor–liquid phase equilibrium, it combines the reaction and separation operations,which reduces energy and capital costs and environmental impact. After an overview of the fundamentals, limitations, and scope of reactive distillation, Reactive Distillation Design and Control:
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Uses rigorous models for steady-state design and dynamic analysis of different types of reactive distillation columns
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Quantitatively compares the economics of reactive distillation columns with conventional multi-unit processes
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Goes beyond traditional steady-state design that considers primarily the capital investment andenergy costs when analyzing the control structure and the dynamic robustness of disturbances
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Discusses how to maximize the economic and environmental benefits of reactive distillation technology
Written by authors who have a background in design and control with an emphasis on practical engineering solutions to real industrial problems, this guide forgoes intricate, complicated mathematics and complex methods of analysis and gets down to business. It's an accessible reference for chemical, process, and petroleum engineers and undergraduate and graduate students in chemical engineering.
Inhalt
Preface xvii
1 Introduction 1
1.1 History 2
1.2 Basics of Reactive Distillation 3
1.3 Neat Operation Versus Excess Reactant 7
1.4 Limitations 8
1.4.1 Temperature Mismatch 8
1.4.2 Unfavorable Volatilities 9
1.4.3 Slow Reaction Rates 9
1.4.4 Other Restrictions 9
1.5 Scope 9
1.6 Computational Methods 10
1.6.1 Matlab Programs for Steady-State Design 10
1.6.2 Aspen Simulations 10
1.7 Reference Materials 11
Part I Steady-State Design of Ideal Quaternary System 15
2 Parameter Effects 17
2.1 Effect of Holdup on Reactive Trays 20
2.2 Effect of Number of Reactive Trays 22
2.3 Effect of Pressure 24
2.4 Effect of Chemical Equilibrium Constant 27
2.5 Effect of Relative Volatilities 29
2.5.1 Constant Relative Volatilities 30
2.5.2 Temperature-Dependent Relative Volatilities 30
2.6 Effect of Number of Stripping and Rectifying Trays 32
2.7 Effect of Reactant Feed Location 33
2.7.1 Reactant A Feed Location (NFA) 33
2.7.2 Reactant B Feed Location (NFB) 35
2.8 Conclusion 36
3 Economic Comparison of Reactive Distillation with a Conventional Process 37
3.1 Conventional Multiunit Process 38
3.1.1 Assumptions and Specifications 38
3.1.2 Steady-State Design Procedure 40
3.1.3 Sizing and Economic Equations 42
3.2 Reactive Distillation Design 43
3.2.1 Assumptions and Specifications 44
3.2.2 Steady-State Design Procedure 45
3.3 Results for Different Chemical Equilibrium Constants 47
3.3.1 Conventional Process 47
3.3.2 Reactive Distillation Process 54
3.3.3 Comparisons 61
3.4 Results for Temperature-Dependent Relative Volatilities 61
3.4.1 Relative Volatilities 62
3.4.2 Optimum Steady-State Designs 64
3.4.3 Real Chemical Systems 69
3.5 Conclusion 70
4 Neat Operation Versus Using Excess Reactant 71
4.1 Introduction 72
4.2 Neat Reactive Column 72
4.3 Two-Column System with Excess B 75
4.3.1 20% Excess B Case 76
4.3.2 10% Excess B Case 78
4.4 Two-Column System with 20% Excess of A 81
4.5 Economic Comparison 85
4.6 Conclusion 86
Part II Steady-State Design of Other Ideal Systems 87
5 Ternary Reactive Distillation Systems 89
5.1 Ternary System without Inerts 90
5.1.1 Column Configuration 90
5.1.2 Chemistry and Phase Equilibrium Parameters 90
5.1.3 Design Parameters and Procedure 92
5.1.4 Effect of Pressure 94
5.1.5 Holdup on Reactive Trays 94
5.1.6 Number of Reactive Trays 94
5.1.7 Number of Stripping Trays 94
5.2 Ternary System with Inerts 99
5.2.1 Column Configuration 99
5.2.2 Chemistry and Phase Equilibrium Parameters 99
5.2.3 Design Parameters and Procedure 100
5.2.4 Effect of Pressure 102
5.2.5 Control Tray Composition 103
5.2.6 Reactive Tray Holdup 105
5.2.7 Effect of Reflux 107
5.2.8 Chemical Equilibrium Constant 109
5.2.9 Feed Composition 109
5.2.10 Number of Reactive Trays 113
5.2.11 Number of Rectifying and Stripping Trays 113
5.3 Conclusion 116
6 Ternary Decomposition Reaction 119
6.1 Ternary Decomposition Reaction: Intermediate-Boiling Reactant 120
6.1.1 Column Configuration 120
6.1.2 Chemistry and Phase Equilibrium Parameters 120
6.1.3 Design Parameters and Procedure 121
6.1.4 Holdup on Reactive Trays 123
6.1.5 Number of Reactive Trays 124
6.1.6 Number of Rectifying and Stripping Trays 126
6.1.7 Location of Feed Tray 126
6.2 Ternary Decomposition Reaction: Heavy Reactant with Two-Column Configurations 127
6.2.1 Column Configurations 127
6.2.2 Chemistry and Phase Equilibrium Parameters 128
6.2.3 Design Parameters and Procedure 128
6.2.4 Reactive Holdup 129
6.2.5 Number of Reactive Trays 131
6.2.6 Number of Rectifying Trays 132
6.3 Ternary Decomposition Reaction: Heavy Reactant with One-Column Configurations 134
6.3.1 Feasibility Analysis 134
6.3.2 Column Configuration 139
6.3.3 Design Parameters and Procedure 139
6.3.4 Reactive Tray Holdup 139
6.3.5 Number of Reactive Trays 139
6.3.6 Number of Rectifying Trays 140
6.3.7 Location of Feed Tray 143
6.3.8 Comparison Between These Two Flowsheets 143
6.4 Conclusion 143
Part III Steady-State Design of Real Chemical Systems 145
7 Steady-State Design for Acetic Acid Esterification 147
7.1 Reaction Kinetics and Phase Equilibria 147
7.1.1 Reaction Kinetics 147
7.1.2 Phase Equilibria 149
7.2 Process Flowsheets 153
7.2.1 Type I Flowshe…