Reactive Distillation Design and Control

Name: Reactive Distillation Design and Control
Brand: Wiley-AIChE
Price: 152.99 EUR
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William L. Luyben Cheng-Ching Yu(Autor*in)

Wiley-AIChE (Verlag)

Erschienen am 31. März 2009

580 Seiten

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978-0-470-37779-6 (ISBN)

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Inhalt

Intro
REACTIVE DISTILLATION DESIGN AND CONTROL
CONTENTS
PREFACE
1 INTRODUCTION
1.1 History
1.2 Basics of Reactive Distillation
1.3 Neat Operation Versus Excess Reactant
1.4 Limitations
1.4.1 Temperature Mismatch
1.4.2 Unfavorable Volatilities
1.4.3 Slow Reaction Rates
1.4.4 Other Restrictions
1.5 Scope
1.6 Computational Methods
1.6.1 Matlab Programs for Steady-State Design
1.6.2 Aspen Simulations
1.7 Reference Materials
PART I STEADY-STATE DESIGN OF IDEAL QUATERNARY SYSTEM
2 PARAMETER EFFECTS
2.1 Effect of Holdup on Reactive Trays
2.2 Effect of Number of Reactive Trays
2.3 Effect of Pressure
2.4 Effect of Chemical Equilibrium Constant
2.5 Effect of Relative Volatilities
2.5.1 Constant Relative Volatilities
2.5.2 Temperature-Dependent Relative Volatilities
2.6 Effect of Number of Stripping and Rectifying Trays
2.7 Effect of Reactant Feed Location
2.7.1 Reactant A Feed Location (N(FA))
2.7.2 Reactant B Feed Location (N(FB))
2.8 Conclusion
3 ECONOMIC COMPARISON OF REACTIVE DISTILLATION WITH A CONVENTIONAL PROCESS
3.1 Conventional Multiunit Process
3.1.1 Assumptions and Specifications
3.1.2 Steady-State Design Procedure
3.1.3 Sizing and Economic Equations
3.2 Reactive Distillation Design
3.2.1 Assumptions and Specifications
3.2.2 Steady-State Design Procedure
3.3 Results for Different Chemical Equilibrium Constants
3.3.1 Conventional Process
3.3.2 Reactive Distillation Process
3.3.3 Comparisons
3.4 Results for Temperature-Dependent Relative Volatilities
3.4.1 Relative Volatilities
3.4.2 Optimum Steady-State Designs
3.4.3 Real Chemical Systems
3.5 Conclusion
4 NEAT OPERATION VERSUS USING EXCESS REACTANT
4.1 Introduction
4.2 Neat Reactive Column
4.3 Two-Column System with Excess B
4.3.1 20% Excess B Case
4.3.2 10% Excess B Case
4.4 Two-Column System with 20% Excess of A
4.5 Economic Comparison
4.6 Conclusion
PART II STEADY-STATE DESIGN OF OTHER IDEAL SYSTEMS
5 TERNARY REACTIVE DISTILLATION SYSTEMS
5.1 Ternary System Without Inerts
5.1.1 Column Configuration
5.1.2 Chemistry and Phase Equilibrium Parameters
5.1.3 Design Parameters and Procedure
5.1.4 Effect of Pressure
5.1.5 Holdup on Reactive Trays
5.1.6 Number of Reactive Trays
5.1.7 Number of Stripping Trays
5.2 Ternary System With Inerts
5.2.1 Column Configuration
5.2.2 Chemistry and Phase Equilibrium Parameters
5.2.3 Design Parameters and Procedure
5.2.4 Effect of Pressure
5.2.5 Control Tray Composition
5.2.6 Reactive Tray Holdup
5.2.7 Effect of Reflux
5.2.8 Chemical Equilibrium Constant
5.2.9 Feed Composition
5.2.10 Number of Reactive Trays
5.2.11 Number of Rectifying and Stripping Trays
5.3 Conclusion
6 TERNARY DECOMPOSITION REACTION
6.1 Ternary Decomposition Reaction: Intermediate-Boiling Reactant
6.1.1 Column Configuration
6.1.2 Chemistry and Phase Equilibrium Parameters
6.1.3 Design Parameters and Procedure
6.1.4 Holdup on Reactive Trays
6.1.5 Number of Reactive Trays
6.1.6 Number of Rectifying and Stripping Trays
6.1.7 Location of Feed Tray
6.2 Ternary Decomposition Reaction: Heavy Reactant with Two-Column Configurations
6.2.1 Column Configurations
6.2.2 Chemistry and Phase Equilibrium Parameters
6.2.3 Design Parameters and Procedure
6.2.4 Reactive Holdup
6.2.5 Number of Reactive Trays
6.2.6 Number of Rectifying Trays
6.3 Ternary Decomposition Reaction: Heavy Reactant with One-Column Configurations
6.3.1 Feasibility Analysis
6.3.2 Column Configuration
6.3.3 Design Parameters and Procedure
6.3.4 Reactive Tray Holdup
6.3.5 Number of Reactive Trays
6.3.6 Number of Rectifying Trays
6.3.7 Location of Feed Tray
6.3.8 Comparison Between These Two Flowsheets
6.4 Conclusion
PART III STEADY-STATE DESIGN OF REAL CHEMICAL SYSTEMS
7 STEADY-STATE DESIGN FOR ACETIC ACID ESTERIFICATION
7.1 Reaction Kinetics and Phase Equilibria
7.1.1 Reaction Kinetics
7.1.2 Phase Equilibria
7.2 Process Flowsheets
7.2.1 Type I Flowsheet: MeAc
7.2.2 Type II Flowsheet: EtAc and IPAc
7.2.3 Type III Flowsheet: BuAc and AmAc
7.3 Steady-State Design
7.3.1 Design Procedure
7.3.2 Optimized Design
7.4 Process Characteristics
7.4.1 Type I: MeAc
7.4.2 Type II: EtAc and IPAc
7.4.3 Type III: BuAc and AmAc
7.5 Discussion
7.6 Conclusion
8 DESIGN OF TAME REACTIVE DISTILLATION SYSTEMS
8.1 Chemical Kinetics and Phase Equilibrium
8.1.1 Chemical Kinetics
8.1.2 Phase Equilibrium Using Aspen Plus
8.1.3 Conceptual Design
8.2 Component Balances
8.3 Prereactor and Reactive Column
8.3.1 Base Case Design of Reactive Column
8.3.2 Effect of Design Parameters on Reactive Column
8.4 Pressure-Swing Methanol Separation Section
8.5 Extractive Distillation Methanol Separation Section
8.6 Economic Comparison
8.7 Conclusion
9 DESIGN OF MTBE AND ETBE REACTIVE DISTILLATION COLUMNS
9.1 MTBE Process
9.1.1 Phase Equilibrium
9.1.2 Reaction Kinetics
9.1.3 Aspen Plus Simulation Issues
9.1.4 Setting up the Aspen Plus Simulation
9.1.5 Effect of Design Parameters
9.1.6 Chemical Equilibrium Model
9.2 ETBE Process
9.2.1 Kinetic Model
9.2.2 Process Studied
9.2.3 User Subroutine for ETBE
9.2.4 Chemical Equilibrium Model
9.2.5 Effects of Design Parameters
9.3 Conclusion
PART IV CONTROL OF IDEAL SYSTEMS
10 CONTROL OF QUATERNARY REACTIVE DISTILLATION COLUMNS
10.1 Introduction
10.2 Steady-State Design
10.3 Control Structures
10.4 Selection of Control Tray Location
10.5 Closed-Loop Performance
10.5.1 CS7-R Structure
10.5.2 CS7-RR Structure
10.6 Using More Reactive Trays
10.6.1 Steady-State Design
10.6.2 SVD Analysis
10.6.3 Dynamic Performance of CS7-RR
10.7 Increasing Holdup on Reactive Trays
10.8 Rangeability
10.9 Conclusion
11 CONTROL OF EXCESS REACTANT SYSTEMS
11.1 Control Degrees of Freedom
11.2 Single Reactive Column Control Structures
11.2.1 Two-Temperature Control Structure
11.2.2 Internal Composition Control Structure
11.3 Control of Two-Column System
11.3.1 Two-Temperature Control
11.3.2 Temperature/Composition Cascade Control
11.4 Conclusion
12 CONTROL OF TERNARY REACTIVE DISTILLATION COLUMNS
12.1 Ternary System Without Inerts
12.1.1 Column Configuration
12.1.2 Control Structure CS1
12.1.3 Control Structure CS2
12.1.4 Control Structure CS3
12.2 Ternary System With Inerts
12.2.1 Column Configuration
12.2.2 Control Structure CS1
12.2.3 Control Structure CS2
12.2.4 Control Structure CS3
12.2.5 Conclusion for Ternary A + B C System
12.3 Ternary A B + C System: Intermediate-Boiling Reactant
12.3.1 Column Configuration
12.3.2 Control Structure CS1
12.3.3 Control Structure CS2
12.3.4 Control Structure CS3
12.4 Ternary A B + C System: Heavy Reactant With Two-Column Configuration
12.4.1 Column Configuration
12.4.2 Control Structure CS1
12.4.3 Control Structure CS2
12.5 Ternary A B + C System: Heavy Reactant With One-Column Configuration
12.5.1 Column Configuration
12.5.2 Control Structure CS1
12.5.3 Control Structure CS2
12.5.4 Control Structure CS3
12.5.5 Conclusion for Ternary A B + C System
PART V CONTROL OF REAL SYSTEMS
13 CONTROL OF REACTIVE DISTILLATIONS FOR ACETIC ACID ESTERIFICATION
13.1 Process Characteristics
13.1.1 Process Studies
13.1.2 Quantitative Analysis
13.2 Control Structure Design
13.2.1 Selection of Temperature Control Trays
13.2.2 Control Structure and Controller Design
13.2.3 Performance
13.2.4 Alternative Temperature Control Structures
13.3 Extension to Composition Control
13.4 Conclusion
14 PLANTWIDE CONTROL OF TAME REACTIVE DISTILLATION SYSTEM
14.1 Process Studied
14.1.1 Prereactor
14.1.2 Reactive Column C1
14.1.3 Extractive Column C2
14.1.4 Methanol Recovery Column C3
14.2 Control Structure
14.2.1 Prereactor
14.2.2 Reactive Distillation Column C1
14.2.3 Extractive Distillation Column C2
14.2.4 Methanol Recovery Column C3
14.3 Results
14.4 Conclusion
15 CONTROL OF MTBE AND ETBE REACTIVE DISTILLATION COLUMNS
15.1 MTBE Control
15.1.1 Steady State
15.1.2 Control Structure with C4 Feedflow Controlled
15.1.3 Control Structure with Methanol Feedflow Controlled
15.2 ETBE Control
15.2.1 Control Structure with Flow Control of C4 Feed
15.2.2 Control Structure with Flow Control of Ethanol Feed
PART VI HYDRID AND NONCONVENTIONAL SYSTEMS
16 DESIGN AND CONTROL OF COLUMN/SIDE REACTOR SYSTEMS
16.1 Introduction
16.2 Design for Quaternary Ideal System
16.2.1 Assumptions and Specifications
16.2.2 Reactor and Column Equations
16.2.3 Design Optimization Procedure
16.2.4 Results and Discussion
16.2.5 Reactive Column with Optimum Feed Tray Locations
16.3 Control of Quaternary Ideal System
16.3.1 Dynamic Tubular Reactor Model
16.3.2 Control Structures
16.4 Design of Column/Side Reactor Process for Ethyl Acetate System
16.4.1 Process Description
16.4.2 Conceptual Design
16.5 Control of Column/Side Reactor Process for Ethyl Acetate System
16.5.1 Determining Manipulated Variables
16.5.2 Selection of Temperature Control Trays
16.5.3 Controller Design
16.5.4 Performance
16.5.5 Extension to Composition Control
16.5.6 Comparison with Reactive Distillation Temperature Control
16.6 Conclusion
17 EFFECTS OF BOILING POINT RANKINGS ON THE DESIGN OF REACTIVE DISTILLATION
17.1 Process and Classification
17.1.1 Process
17.1.2 Classification
17.2 Relaxation and Convergence
17.3 Process Configurations
17.3.1 Type I: One Group
17.3.2 Type II: Two Groups
17.3.3 Type III: Alternating
17.4 Results and Discussion
17.4.1 Summary
17.4.2 Excess Reactant Design
17.5 Conclusion
18 EFFECTS OF FEED TRAY LOCATIONS ON DESIGN AND CONTROL OF REACTIVE DISTILLATION
18.1 Process Characteristics
18.1.1 Modeling
18.1.2 Steady-State Design
18.1.3 Base Case
18.1.4 Feed Locations Versus Reactants Distribution
18.1.5 Optimal Feed Locations
18.2 Effects of Relative Volatilities
18.2.1 Changing Relative Volatilities of Reactants
18.2.2 Changing Relative Volatilities of Products
18.2.3 Summary
18.3 Effects of Reaction Kinetics
18.3.1 Reducing Activation Energies
18.3.2 Effects of Preexponential Factor
18.4 Operation and Control
18.4.1 Optimal Feed Location for Production Rate Variation
18.4.2 Control Structure
18.4.3 Closed-Loop Performance
18.5 Conclusion
APPENDIX CATALOG OF TYPES OF REAL REACTIVE DISTILLATION SYSTEMS
REFERENCES
INDEX

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