William L. Luyben

Distillation Simulation, 2e

• Gebundenes Buch

Produktbeschreibung

The new edition of this book greatly updates and expands the previous edition. It boasts new chapters on the divided wall column and carbon dioxide capture from stack gas, revises the design and control of distillation systems, and explains the use of dynamic simulation to study safety issues in the event of operating failures. Using Aspen Plus to develop rigorous simulations of single distillation columns and sequences of columns, the book considers the economics of capital investment and energy costs to create an optimal system for separation methods in the chemical and petroleum industries.

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Learn how to develop optimal steady-state designs for distillation systems

As the search for new energy sources grows ever more urgent, distillation remains at the forefront among separation methods in the chemical, petroleum, and energy industries. Most importantly, as renewable sources of energy and chemical feedstocks continue to be developed, distillation design and control will become ever more important in our ability to ensure global sustainability.

Using the commercial simulators Aspen Plus(r) and Aspen Dynamics(r), this text enables readers to develop optimal steady-state designs for distillation systems. Moreover, readers will discover how to develop effective control structures. While traditional distillation texts focus on the steady-state economic aspects of distillation design, this text also addresses such issues as dynamic performance in the face of disturbances.

Distillation Design and Control Using Aspen(tm) Simulation introduces the current status and future implications of this vital technology from the perspectives of steady-state design and dynamics. The book begins with a discussion of vapor-liquid phase equilibrium and then explains the core methods and approaches for analyzing distillation columns. Next, the author covers such topics as:
Setting up a steady-state simulation
Distillation economic optimization
Steady-state calculations for control structure selection
Control of petroleum fractionators
Design and control of divided-wall columns
Pressure-compensated temperature control in distillation columns

Synthesizing four decades of research breakthroughs and practical applications in this dynamic field, Distillation Design and Control Using Aspen(tm) Simulation is a trusted reference that enables both students and experienced engineers to solve a broad range of challenging distillation problems.

Produktdetails

• Verlag: Wiley & Sons
• Artikelnr. des Verlages: 1W118411430
• 2. Aufl.
• Seitenzahl: 512
• Erscheinungstermin: 29. April 2013
• Englisch
• Abmessung: 260mm x 183mm x 32mm
• Gewicht: 1060g
• ISBN-13: 9781118411438
• ISBN-10: 1118411439
• Artikelnr.: 37226559

Autorenporträt

WILLIAM L. LUYBEN, PhD, is Professor of Chemical Engineering at Lehigh University where he has taught for over forty-five years. Dr. Luyben spent nine years as an engineer with Exxon and DuPont. He has published fourteen books and more than 250 original research papers. Dr. Luyben is a 2003 recipient of the Computing Practice Award from the CAST Division of the AIChE. He was elected to the Process Control Hall of Fame in 2005. In 2011, the Separations Division of the AIChE recognized his contributions to distillation technology by a special honors session.

Inhaltsangabe

PREFACE TO THE SECOND EDITION xv PREFACE TO THE FIRST EDITION xvii 1 FUNDAMENTALS OF VAPOR-LIQUID-EQUILIBRIUM (VLE) 1 1.1 Vapor Pressure
1 1.2 Binary VLE Phase Diagrams
3 1.3 Physical Property Methods
7 1.4 Relative Volatility
7 1.5 Bubble Point Calculations
8 1.6 Ternary Diagrams
9 1.7 VLE Nonideality
11 1.8 Residue Curves for Ternary Systems
15 1.9 Distillation Boundaries
22 1.10 Conclusions
25 Reference
27 2 ANALYSIS OF DISTILLATION COLUMNS 29 2.1 Design Degrees of Freedom
29 2.2 Binary McCabe-Thiele Method
30 2.2.1 Operating Lines
32 2.2.2 q-Line
33 2.2.3 Stepping Off Trays
35 2.2.4 Effect of Parameters
35 2.2.5 Limiting Conditions
36 2.3 Approximate Multicomponent Methods
36 2.3.1 Fenske Equation for Minimum Number of Trays
37 2.3.2 Underwood Equations for Minimum Reflux Ratio
37 2.4 Conclusions
38 3 SETTING UP A STEADY-STATE SIMULATION 39 3.1 Configuring a New Simulation
39 3.2 Specifying Chemical Components and Physical Properties
46 3.3 Specifying Stream Properties
51 3.4 Specifying Parameters of Equipment
52 3.4.1 Column C1
52 3.4.2 Valves and Pumps
55 3.5 Running the Simulation
57 3.6 Using Design Spec
Vary Function
58 3.7 Finding the Optimum Feed Tray and Minimum Conditions
70 3.7.1 Optimum Feed Tray
70 3.7.2 Minimum Reflux Ratio
71 3.7.3 Minimum Number of Trays
71 3.8 Column Sizing
72 3.8.1 Length
72 3.8.2 Diameter
72 3.9 Conceptual Design
74 3.10 Conclusions
80 4 DISTILLATION ECONOMIC OPTIMIZATION 81 4.1 Heuristic Optimization
81 4.1.1 Set Total Trays to Twice Minimum Number of Trays
81 4.1.2 Set Reflux Ratio to 1.2 Times Minimum Reflux Ratio
83 4.2 Economic Basis
83 4.3 Results
85 4.4 Operating Optimization
87 4.5 Optimum Pressure for Vacuum Columns
92 4.6 Conclusions
94 5 MORE COMPLEX DISTILLATION SYSTEMS 95 5.1 Extractive Distillation
95 5.1.1 Design
99 5.1.2 Simulation Issues
101 5.2 Ethanol Dehydration
105 5.2.1 VLLE Behavior
106 5.2.2 Process Flowsheet Simulation
109 5.2.3 Converging the Flowsheet
112 5.3 Pressure-Swing Azeotropic Distillation
115 5.4 Heat-Integrated Columns
121 5.4.1 Flowsheet
121 5.4.2 Converging for Neat Operation
122 5.5 Conclusions
126 6 STEADY-STATE CALCULATIONS FOR CONTROL STRUCTURE SELECTION 127 6.1 Control Structure Alternatives
127 6.1.1 Dual-Composition Control
127 6.1.2 Single-End Control
128 6.2 Feed Composition Sensitivity Analysis (ZSA)
128 6.3 Temperature Control Tray Selection
129 6.3.1 Summary of Methods
130 6.3.2 Binary Propane
Isobutane System
131 6.3.3 Ternary BTX System
135 6.3.4 Ternary Azeotropic System
139 6.4 Conclusions
144 Reference
144 7 CONVERTING FROM STEADY-STATE TO DYNAMIC SIMULATION 145 7.1 Equipment Sizing
146 7.2 Exporting to Aspen Dynamics
148 7.3 Opening the Dynamic Simulation in Aspen Dynamics
150 7.4 Installing Basic Controllers
152 7.4.1 Reflux
156 7.4.2 Issues
157 7.5 Installing Temperature and Composition Controllers
161 7.5.1 Tray Temperature Control
162 7.5.2 Composition Control
170 7.5.3 Composition
Temperature Cascade Control
170 7.6 Performance Evaluation
172 7.6.1 Installing a Plot
172 7.6.2 Importing Dynamic Results into Matlab
174 7.6.3 Reboiler Heat Input to Feed Ratio
176 7.6.4 Comparison of Temperature Control with Cascade CC
TC
181 7.7 Conclusions
184 8 CONTROL OF MORE COMPLEX COLUMNS 185 8.1 Extractive Distillation Process
185 8.1.1 Design
185 8.1.2 Control Structure
188 8.1.3 Dynamic Performance
191 8.2 Columns with Partial Condensers
191 8.2.1 Total Vapor Distillate
192 8.2.2 Both Vapor and Liquid Distillate Streams
209 8.3 Control of Heat-Integrated Distillation Columns
217 8.3.1 Process Studied
217 8.3.2 Heat Integration Relationships
218 8.3.3 Control Structure
222 8.3.4 Dynamic Performance
223 8.4 Control of Azeotropic Columns
Decanter System
226 8.4.1 Converting to Dynamics and Closing Recycle Loop
227 8.4.2 Installing the Control Structure
228 8.4.3 Performance
233 8.4.4 Numerical Integration Issues
237 8.5 Unusual Control Structure
238 8.5.1 Process Studied
239 8.5.2 Economic Optimum Steady-State Design
242 8.5.3 Control Structure Selection
243 8.5.4 Dynamic Simulation Results
248 8.5.5 Alternative Control Structures
248 8.5.6 Conclusions
254 8.6 Conclusions
255 References
255 9 REACTIVE DISTILLATION 257 9.1 Introduction
257 9.2 Types of Reactive Distillation Systems
258 9.2.1 Single-Feed Reactions
259 9.2.2 Irreversible Reaction with Heavy Product
259 9.2.3 Neat Operation Versus Use of Excess Reactant
260 9.3 TAME Process Basics
263 9.3.1 Prereactor
263 9.3.2 Reactive Column C1
263 9.4 TAME Reaction Kinetics and VLE
266 9.5 Plantwide Control Structure
270 9.6 Conclusions
274 References
274 10 CONTROL OF SIDESTREAM COLUMNS 275 10.1 Liquid Sidestream Column
276 10.1.1 Steady-State Design
276 10.1.2 Dynamic Control
277 10.2 Vapor Sidestream Column
281 10.2.1 Steady-State Design
282 10.2.2 Dynamic Control
282 10.3 Liquid Sidestream Column with Stripper
286 10.3.1 Steady-State Design
286 10.3.2 Dynamic Control
288 10.4 Vapor Sidestream Column with Rectifier
292 10.4.1 Steady-State Design
292 10.4.2 Dynamic Control
293 10.5 Sidestream Purge Column
300 10.5.1 Steady-State Design
300 10.5.2 Dynamic Control
302 10.6 Conclusions
307 11 CONTROL OF PETROLEUM FRACTIONATORS 309 11.1 Petroleum Fractions
310 11.2 Characterization Crude Oil
314 11.3 Steady-State Design of Preflash Column
321 11.4 Control of Preflash Column
328 11.5 Steady-State Design of Pipestill
332 11.5.1 Overview of Steady-State Design
333 11.5.2 Configuring the Pipestill in Aspen Plus
335 11.5.3 Effects of Design Parameters
344 11.6 Control of Pipestill
346 11.7 Conclusions
354 References
354 12 DIVIDED-WALL (PETLYUK) COLUMNS 355 12.1 Introduction
355 12.2 Steady-State Design
357 12.2.1 MultiFrac Model
357 12.2.2 RadFrac Model
366 12.3 Control of the Divided-Wall Column
369 12.3.1 Control Structure
369 12.3.2 Implementation in Aspen Dynamics
373 12.3.3 Dynamic Results
375 12.4 Control of the Conventional Column Process
380 12.4.1 Control Structure
380 12.4.2 Dynamic Results and Comparisons
381 12.5 Conclusions and Discussion
383 References
384 13 DYNAMIC SAFETY ANALYSIS 385 13.1 Introduction
385 13.2 Safety Scenarios
385 13.3 Process Studied
387 13.4 Basic RadFrac Models
387 13.4.1 Constant Duty Model
387 13.4.2 Constant Temperature Model
388 13.4.3 LMTD Model
388 13.4.4 Condensing or Evaporating Medium Models
388 13.4.5 Dynamic Model for Reboiler
388 13.5 RadFrac Model with Explicit Heat-Exchanger Dynamics
389 13.5.1 Column
389 13.5.2 Condenser
390 13.5.3 Reflux Drum
391 13.5.4 Liquid Split
391 13.5.5 Reboiler
391 13.6 Dynamic Simulations
392 13.6.1 Base Case Control Structure
392 13.6.2 Rigorous Case Control Structure
393 13.7 Comparison of Dynamic Responses
394 13.7.1 Condenser Cooling Failure
394 13.7.2 Heat-Input Surge
395 13.8 Other Issues
397 13.9 Conclusions
398 Reference
398 14 CARBON DIOXIDE CAPTURE 399 14.1 Carbon Dioxide Removal in Low-Pressure Air Combustion Power Plants
400 14.1.1 Process Design
400 14.1.2 Simulation Issues
401 14.1.3 Plantwide Control Structure
404 14.1.4 Dynamic Performance
408 14.2 Carbon Dioxide Removal in High-Pressure IGCC Power Plants
412 14.2.1 Design
414 14.2.2 Plantwide Control Structure
414 14.2.3 Dynamic Performance
418 14.3 Conclusions
420 References
421 15 DISTILLATION TURNDOWN 423 15.1 Introduction
423 15.2 Control Problem
424 15.2.1 Two-Temperature Control
425 15.2.2 Valve-Position Control
426 15.2.3 Recycle Control
427 15.3 Process Studied
428 15.4 Dynamic Performance for Ramp Disturbances
431 15.4.1 Two-Temperature Control
431 15.4.2 VPC Control
432 15.4.3 Recycle Control
433 15.4.4 Comparison
434 15.5 Dynamic Performance for Step Disturbances
435 15.5.1 Two-Temperature Control
435 15.5.2 VPC Control
436 15.5.3 Recycle Control
436 15.6 Other Control Structures
439 15.6.1 No Temperature Control
439 15.6.2 Dual Temperature Control
440 15.7 Conclusions
442 References
442 16 PRESSURE-COMPENSATED TEMPERATURE CONTROL IN DISTILLATION COLUMNS 443 16.1 Introduction
443 16.2 Numerical Example Studied
445 16.3 Conventional Control Structure Selection
446 16.4 Temperature
Pressure
Composition Relationships
450 16.5 Implementation in Aspen Dynamics
451 16.6 Comparison of Dynamic Results
452 16.6.1 Feed Flow Rate Disturbances
452 16.6.2 Pressure Disturbances
453 16.7 Conclusions
455 References
456 17 ETHANOL DEHYDRATION 457 17.1 Introduction
457 17.2 Optimization of the Beer Still (Preconcentrator)
459 17.3 Optimization of the Azeotropic and Recovery Columns
460 17.3.1 Optimum Feed Locations
461 17.3.2 Optimum Number of Stages
462 17.4 Optimization of the Entire Process
462 17.5 Cyclohexane Entrainer
466 17.6 Flowsheet Recycle Convergence
466 17.7 Conclusions
467 References
467 18 EXTERNAL RESET FEEDBACK TO PREVENT RESET WINDUP 469 18.1 Introduction
469 18.2 External Reset Feedback Circuit Implementation
471 18.2.1 Generate the Error Signal
472 18.2.2 Multiply by Controller Gain
472 18.2.3 Add the Output of Lag
472 18.2.4 Select Lower Signal
472 18.2.5 Setting up the Lag Block
472 18.3 Flash Tank Example
473 18.3.1 Process and Normal Control Structure
473 18.3.2 Override Control Structure Without External Reset Feedback
474 18.3.3 Override Control Structure with External Reset Feedback
476 18.4 Distillation Column Example
479 18.4.1 Normal Control Structure
479 18.4.2 Normal and Override Controllers Without External Reset
481 18.4.3 Normal and Override Controllers with External Reset Feedback
483 18.5 Conclusions
486 References
486 INDEX 487