Distillation design and control using Aspen simulation /

• Κύριος συγγραφέας: Luyben, William L.
• Μορφή: Ηλ. βιβλίο
• Γλώσσα: English
• Έκδοση: Hoboken, N.J. : Wiley, [2013]
• Έκδοση: 2nd ed.
• Θέματα: Distillation apparatus > Design and construction.; Chemical process control > Simulation methods.; Petroleum > Refining.; SCIENCE > Chemistry > Industrial & Technical.; TECHNOLOGY & ENGINEERING > Chemical & Biochemical.; Electronic books.

Πίνακας περιεχομένων:

• 1. Fundamentals of Vapor
• Liquid
• Equilibrium (VLE)
• 1.1. Vapor Pressure
• 1.2. Binary VLE Phase Diagrams
• 1.3. Physical Property Methods
• 1.4. Relative Volatility
• 1.5. Bubble Point Calculations
• 1.6. Ternary Diagrams
• 1.7. VLE Nonideality
• 1.8. Residue Curves for Ternary Systems
• 1.9. Distillation Boundaries
• 1.10. Conclusions
• Reference
• 2. Analysis of Distillation Columns
• 2.1. Design Degrees of Freedom
• 2.2. Binary McCabe
• Thiele Method
• 2.2.1. Operating Lines
• 2.2.2.q-Line
• 2.2.3. Stepping Off Trays
• 2.2.4. Effect of Parameters
• 2.2.5. Limiting Conditions
• 2.3. Approximate Multicomponent Methods
• 2.3.1. Fenske Equation for Minimum Number of Trays
• 2.3.2. Underwood Equations for Minimum Reflux Ratio
• 2.4. Conclusions
• 3. Setting Up a Steady-State Simulation
• 3.1. Configuring a New Simulation
• 3.2. Specifying Chemical Components and Physical Properties
• 3.3. Specifying Stream Properties.
• 3.4. Specifying Parameters of Equipment
• 3.4.1. Column C1
• 3.4.2. Valves and Pumps
• 3.5. Running the Simulation
• 3.6. Using Design Spec/Vary Function
• 3.7. Finding the Optimum Feed Tray and Minimum Conditions
• 3.7.1. Optimum Feed Tray
• 3.7.2. Minimum Reflux Ratio
• 3.7.3. Minimum Number of Trays
• 3.8. Column Sizing
• 3.8.1. Length
• 3.8.2. Diameter
• 3.9. Conceptual Design
• 3.10. Conclusions
• 4. Distillation Economic Optimization
• 4.1. Heuristic Optimization
• 4.1.1. Set Total Trays to Twice Minimum Number of Trays
• 4.1.2. Set Reflux Ratio to 1.2 Times Minimum Reflux Ratio
• 4.2. Economic Basis
• 4.3. Results
• 4.4. Operating Optimization
• 4.5. Optimum Pressure for Vacuum Columns
• 4.6. Conclusions
• 5. More Complex Distillation Systems
• 5.1. Extractive Distillation
• 5.1.1. Design
• 5.1.2. Simulation Issues
• 5.2. Ethanol Dehydration
• 5.2.1. VLLE Behavior
• 5.2.2. Process Flowsheet Simulation
• 5.2.3. Converging the Flowsheet.
• 5.3. Pressure-Swing Azeotropic Distillation
• 5.4. Heat-Integrated Columns
• 5.4.1. Flowsheet
• 5.4.2. Converging for Neat Operation
• 5.5. Conclusions
• 6. Steady-State Calculations for Control Structure Selection
• 6.1. Control Structure Alternatives
• 6.1.1. Dual-Composition Control
• 6.1.2. Single-End Control
• 6.2. Feed Composition Sensitivity Analysis (ZSA)
• 6.3. Temperature Control Tray Selection
• 6.3.1. Summary of Methods
• 6.3.2. Binary Propane/Isobutane System
• 6.3.3. Ternary BTX System
• 6.3.4. Ternary Azeotropic System
• 6.4. Conclusions
• Reference
• 7. Converting from Steady-State to Dynamic Simulation
• 7.1. Equipment Sizing
• 7.2. Exporting to Aspen Dynamics
• 7.3. Opening the Dynamic Simulation in Aspen Dynamics
• 7.4. Installing Basic Controllers
• 7.4.1. Reflux
• 7.4.2. Issues
• 7.5. Installing Temperature and Composition Controllers
• 7.5.1. Tray Temperature Control
• 7.5.2.Composition Control.
• 7.5.3.Composition/Temperature Cascade Control
• 7.6. Performance Evaluation
• 7.6.1. Installing a Plot
• 7.6.2. Importing Dynamic Results into Matlab
• 7.6.3. Reboiler Heat Input to Feed Ratio
• 7.6.4.Comparison of Temperature Control with Cascade CC/TC
• 7.7. Conclusions
• 8. Control of More Complex Columns
• 8.1. Extractive Distillation Process
• 8.1.1. Design
• 8.1.2. Control Structure
• 8.1.3. Dynamic Performance
• 8.2. Columns with Partial Condensers
• 8.2.1. Total Vapor Distillate
• 8.2.2. Both Vapor and Liquid Distillate Streams
• 8.3. Control of Heat-Integrated Distillation Columns
• 8.3.1. Process Studied
• 8.3.2. Heat Integration Relationships
• 8.3.3. Control Structure
• 8.3.4. Dynamic Performance
• 8.4. Control of Azeotropic Columns/Decanter System
• 8.4.1. Converting to Dynamics and Closing Recycle Loop
• 8.4.2. Installing the Control Structure
• 8.4.3. Performance
• 8.4.4. Numerical Integration Issues
• 8.5. Unusual Control Structure.
• 8.5.1. Process Studied
• 8.5.2. Economic Optimum Steady-State Design
• 8.5.3. Control Structure Selection
• 8.5.4. Dynamic Simulation Results
• 8.5.5. Alternative Control Structures
• 8.5.6. Conclusions
• 8.6. Conclusions
• References
• 9. Reactive Distillation
• 9.1. Introduction
• 9.2. Types of Reactive Distillation Systems
• 9.2.1. Single-Feed Reactions
• 9.2.2. Irreversible Reaction with Heavy Product
• 9.2.3. Neat Operation Versus Use of Excess Reactant
• 9.3. TAME Process Basics
• 9.3.1. Prereactor
• 9.3.2. Reactive Column C1
• 9.4. TAME Reaction Kinetics and VLE
• 9.5. Plantwide Control Structure
• 9.6. Conclusions
• References
• 10. Control of Sidestream Columns
• 10.1. Liquid Sidestream Column
• 10.1.1. Steady-State Design
• 10.1.2. Dynamic Control
• 10.2. Vapor Sidestream Column
• 10.2.1. Steady-State Design
• 10.2.2. Dynamic Control
• 10.3. Liquid Sidestream Column with Stripper
• 10.3.1. Steady-State Design
• 10.3.2. Dynamic Control.
• 10.4. Vapor Sidestream Column with Rectifier
• 10.4.1. Steady-State Design
• 10.4.2. Dynamic Control
• 10.5. Sidestream Purge Column
• 10.5.1. Steady-State Design
• 10.5.2. Dynamic Control
• 10.6. Conclusions
• 11. Control of Petroleum Fractionators
• 11.1. Petroleum Fractions
• 11.2. Characterization Crude Oil
• 11.3. Steady-State Design of Preflash Column
• 11.4. Control of Preflash Column
• 11.5. Steady-State Design of Pipestill
• 11.5.1. Overview of Steady-State Design
• 11.5.2. Configuring the Pipestill in Aspen Plus
• 11.5.3. Effects of Design Parameters
• 11.6. Control of Pipestill
• 11.7. Conclusions
• References
• 12. Divided-Wall (Petlyuk) Columns
• 12.1. Introduction
• 12.2. Steady-State Design
• 12.2.1. MultiFrac Model
• 12.2.2. RadFrac Model
• 12.3. Control of the Divided-Wall Column
• 12.3.1. Control Structure
• 12.3.2. Implementation in Aspen Dynamics
• 12.3.3. Dynamic Results
• 12.4. Control of the Conventional Column Process.
• 12.4.1. Control Structure
• 12.4.2. Dynamic Results and Comparisons
• 12.5. Conclusions and Discussion
• References
• 13. Dynamic Safety Analysis
• 13.1. Introduction
• 13.2. Safety Scenarios
• 13.3. Process Studied
• 13.4. Basic RadFrac Models
• 13.4.1. Constant Duty Model
• 13.4.2. Constant Temperature Model
• 13.4.3. LMTD Model
• 13.4.4. Condensing or Evaporating Medium Models
• 13.4.5. Dynamic Model for Reboiler
• 13.5. RadFrac Model with Explicit Heat-Exchanger Dynamics
• 13.5.1. Column
• 13.5.2. Condenser
• 13.5.3. Reflux Drum
• 13.5.4. Liquid Split
• 13.5.5. Reboiler
• 13.6. Dynamic Simulations
• 13.6.1. Base Case Control Structure
• 13.6.2. Rigorous Case Control Structure
• 13.7.Comparison of Dynamic Responses
• 13.7.1. Condenser Cooling Failure
• 13.7.2. Heat-Input Surge
• 13.8. Other Issues
• 13.9. Conclusions
• Reference
• 14. Carbon Dioxide Capture
• 14.1. Carbon Dioxide Removal in Low-Pressure Air Combustion Power Plants.
• 14.1.1. Process Design
• 14.1.2. Simulation Issues
• 14.1.3. Plantwide Control Structure
• 14.1.4. Dynamic Performance
• 14.2. Carbon Dioxide Removal in High-Pressure IGCC Power Plants
• 14.2.1. Design
• 14.2.2. Plantwide Control Structure
• 14.2.3. Dynamic Performance
• 14.3. Conclusions
• References
• 15. Distillation Turndown
• 15.1. Introduction
• 15.2. Control Problem
• 15.2.1. Two-Temperature Control
• 15.2.2. Valve-Position Control
• 15.2.3. Recycle Control
• 15.3. Process Studied
• 15.4. Dynamic Performance for Ramp Disturbances
• 15.4.1. Two-Temperature Control
• 15.4.2. VPC Control
• 15.4.3. Recycle Control
• 15.4.4.Comparison
• 15.5. Dynamic Performance for Step Disturbances
• 15.5.1. Two-Temperature Control
• 15.5.2. VPC Control
• 15.5.3. Recycle Control
• 15.6. Other Control Structures
• 15.6.1. No Temperature Control
• 15.6.2. Dual Temperature Control
• 15.7. Conclusions
• References.
• 16. Pressure-Compensated Temperature Control in Distillation Columns
• 16.1. Introduction
• 16.2. Numerical Example Studied
• 16.3. Conventional Control Structure Selection
• 16.4. Temperature/Pressure/Composition Relationships
• 16.5. Implementation in Aspen Dynamics
• 16.6.Comparison of Dynamic Results
• 16.6.1. Feed Flow Rate Disturbances
• 16.6.2. Pressure Disturbances
• 16.7. Conclusions
• References
• 17. Ethanol Dehydration
• 17.1. Introduction
• 17.2. Optimization of the Beer Still (Preconcentrator)
• 17.3. Optimization of the Azeotropic and Recovery Columns
• 17.3.1. Optimum Feed Locations
• 17.3.2. Optimum Number of Stages
• 17.4. Optimization of the Entire Process
• 17.5. Cyclohexane Entrainer
• 17.6. Flowsheet Recycle Convergence
• 17.7. Conclusions
• References
• 18. External Reset Feedback to Prevent Reset Windup
• 18.1. Introduction
• 18.2. External Reset Feedback Circuit Implementation
• 18.2.1. Generate the Error Signal.
• 18.2.2. Multiply by Controller Gain
• 18.2.3. Add the Output of Lag
• 18.2.4. Select Lower Signal
• 18.2.5. Setting up the Lag Block
• 18.3. Flash Tank Example
• 18.3.1. Process and Normal Control Structure
• 18.3.2. Override Control Structure Without External Reset Feedback
• 18.3.3. Override Control Structure with External Reset Feedback
• 18.4. Distillation Column Example
• 18.4.1. Normal Control Structure
• 18.4.2. Normal and Override Controllers Without External Reset
• 18.4.3. Normal and Override Controllers with External Reset Feedback
• 18.5. Conclusions
• References.