Distillation : Principles and Practice

• Record Nr.: UNINA9910555001503321
• Autore: Stichlmair Johann G
• Pubbl/distr/stampa: Newark : , : American Institute of Chemical Engineers, , 2021; ©2021
• ISBN: 1-5231-4336-3; 1-119-41468-7; 1-119-41469-5; 1-119-41467-9
• Edizione: [2nd ed.]
• Descrizione fisica: 1 online resource (685 pages)
• Altri autori (Persone): KleinHarald; RehfeldtSebastian
• Disciplina: 660/.28425
• Soggetti: Electronic books.
• Lingua di pubblicazione: Inglese
• Formato: Materiale a stampa
• Livello bibliografico: Monografia
• Nota di contenuto: Cover -- Title Page -- Copyright -- Contents -- Preface -- Nomenclature -- 1 Introduction -- 1.1 Principle of Distillation Separation -- 1.2 Historical -- 2 Vapor-Liquid Equilibrium -- 2.1 Basic Thermodynamic Correlations -- 2.1.1 Measures of Concentration -- 2.1.2 Equations of State (EOS) -- 2.1.3 Molar Mixing and Partial Molar State Variables -- 2.1.4 Saturation Vapor Pressure and Boiling Temperature of Pure Components -- 2.1.5 Fundamental Equation and the Chemical Potential -- 2.1.6 Gibbs-Duhem Equation and Gibbs-Helmholtz Equation -- 2.2 Calculation of Vapor-Liquid Equilibrium in Mixtures -- 2.2.1 Basic Equilibrium Conditions -- 2.2.2 Gibbs Phase Rule -- 2.2.3 Correlations for the Chemical Potential -- 2.2.4 Calculating Activity Coefficients with the Molar Excess Free Energy -- 2.2.5 Thermodynamic Consistency Check of Molar Excess Free Energy and Activity Coefficients -- 2.2.6 Iso-fugacity Condition -- 2.2.7 Fugacity of the Liquid Phase -- 2.2.8 Fugacity of the Vapor Phase -- 2.2.9 Vapor-Liquid Equilibrium Using an Equation of St -- 2.2.10 Fugacity of Pure Liquid as Standard Fugacity: Raoult's Law -- 2.2.11 Fugacity of Infinitely Diluted Component as Standard Fugacity: Henry's Law -- 2.2.12 Correlations Describing the Molar Excess Free Energy ; and Activity Coefficients -- 2.2.13 Using Experimental Data of Binary Mixtures for Correlations Describing the Molar Excess Free Energy and Activity Coefficients -- 2.2.14 Vapor-Liquid Equilibrium Ratio of Mixtures -- 2.2.15 Relative Volatility of Mixtures -- 2.2.16 Boiling Condition of Liquid Mixtures -- 2.2.17 Condensation (Dew Point) Condition of Vapor Mixtures -- 2.3 Binary Mixtures and Phase Diagrams -- 2.3.1 Boiling Curve Correlation -- 2.3.2 Condensation (Dew Point) Curve Correlation -- 2.3.3 (p, x, y)-Diagram -- 2.3.4 (T, x, y)-Diagram -- 2.3.5 McCabe-Thiele Diagram.; 2.3.6 Boiling and Condensation Behavior of Binary Mixtures -- 2.3.7 General Aspects of Azeotropic Mixtures -- 2.3.8 Limiting Cases of Binary Mi -- 2.4 Ternary Mixtures -- 2.4.1 Boiling and Condensation Conditions of Ternary Mixtures -- 2.4.2 Triangular Diagrams -- 2.4.3 Boiling Surfaces -- 2.4.4 Condensation Surfaces -- 2.4.5 Derivation of Distillation Lines -- 2.4.6 Examples for Distillation Lines -- 3 Single-Stage Distillation and Condensation -- 3.1 Continuous Closed Distillation and Condensation -- 3.1.1 Closed Distillation of Binary Mixtures -- 3.1.2 Closed Distillation of Multicomponent Mixtures -- 3.2 Batchwise Open Distillation and Open Condensation -- 3.2.1 Binary Mixtures -- 3.2.2 Ternary Mixtures -- 3.2.3 Multicomponent Mixtures -- 3.3 Semi-continuous Single-Stage Distillation -- 3.3.1 Semi-continuous Single-Stage Distillation of Binary Mixtures -- 4 Multistage Continuous Distillation (Rectification) -- 4.1 Principles -- 4.1.1 Equilibrium-Stage Concept -- 4.1.2 Transfer-Unit Concept -- 4.1.3 Comparison of Equilibrium-Stage and Transfer-Unit Concepts -- 4.2 Multistage Distillation of Binary Mixtures -- 4.2.1 Calculations Based on Material Bal -- 4.2.2 Calculation Based on Material and Enthalpy Balances -- 4.2.3 Distillation of Binary Mixtures at Total Reflux and Reboil -- 4.2.4 Distillation of Binary Mixtures at Minimum Reflux and Reboil -- 4.2.5 Energy Requirement for Distillation of Binary Mixtures -- 4.3 Multistage Distillation of Ternary Mixtures -- 4.3.1 Calculations Based on Material Balances -- 4.3.2 Distillation of Ternary Mixtures at Total Reflux and Reboil -- 4.3.3 Distillation of Ternary Mixtures at Minimum Reflux and Reboil -- 4.3.4 Energy Requirement of Ternary Distillation -- 4.4 Multistage Distillation of Multicomponent Mixtures -- 4.4.1 Rigorous Column Simulation -- 5 Reactive Distillation, Catalytic Distillation.; 5.1 Fundamentals -- 5.1.1 Chemical Equilibrium -- 5.1.2 Stoichiometric Lines -- 5.1.3 Non-reactive and Reactive Distillation Lines -- 5.1.4 Reactive Azeotropes -- 5.2 Topology of Reactive Distillation Lines -- 5.2.1 Reactions in Ternary Systems -- 5.2.2 Reactions in Ternary Systems with Inert Components -- 5.2.3 Reactions with Side Products -- 5.2.4 Reactions in Quaternary Systems -- 5.3 Topology of Reactive Distillation Processes -- 5.3.1 Single Product Reactions -- 5.3.2 Decomposition Reactions -- 5.3.3 Side Reactions -- 5.4 Arrangement of Catalysts in Columns -- 5.4.1 Homogeneous Catalyst -- 5.4.2 Heterogeneous Catalyst -- 6 Multistage Batch Distillation -- 6.1 Batch Distillation of Binary Mixtures -- 6.1.1 Operation with Constant Reflux -- 6.1.2 Operation with Constant Distillate Composition -- 6.1.3 Operation with Minimum Energy Input -- 6.1.4 Comparison of Energy Requirement for Different Modes of Distillation -- 6.2 Batch Distillation of Ternary Mixtures -- 6.2.1 Zeotropic Mixtures -- 6.2.2 Azeotropic Mixtures -- 6.3 Batch Distillation of Multicomponent Mixtures -- 6.4 Influence of Column Liquid Hold-up on Batch Distillation -- 6.5 Processes for Separating Zeotropic Mixtures by Batch Distillation -- 6.5.1 Total Slop Cut Recycling -- 6.5.2 Binary Distillation of the Accumulated Slop Cuts -- 6.5.3 Recycling of the Slop Cuts at the Appropriate Time -- 6.5.4 Cyclic ; Operation -- 6.6 Processes for Separating Azeotropic Mixtures by Batch Distillation -- 6.6.1 Processes in One Distillation Field -- 6.6.2 Processes in Two Distillation Fields -- 6.6.3 Process Simplifications -- 6.6.4 Hybrid Processes -- 7 Energy Economization in Distillation -- 7.1 Energy Requirement of Single Columns -- 7.1.1 Reduction of Energy Requirement -- 7.1.2 Reduction of Exergy Losses -- 7.2 Optimal Separation Sequences of Ternary Distillation.; 7.2.1 Process and Energy Requirement of the a-Path -- 7.2.2 Process and Energy Requirement of the c-Path -- 7.2.3 Process and Energy Requirement of the Preferred a=c-Path -- 7.3 Modifications of the Basic Processes -- 7.3.1 Material (Direct) Coupling of Columns -- 7.3.2 Processes with Side Columns -- 7.3.3 Thermal (Indirect) Coupling of Columns -- 7.4 Design of Heat Exchanger Networks -- 7.4.1 Optimum Heat Exchanger Networks -- 7.4.2 Modifying the Optimum Heat Exchanger Network -- 7.4.3 Dual Flow Heat Exchanger Networks -- 7.4.4 Process Modifications -- 8 Industrial Distillation Processes -- 8.1 Constraints for Industrial Distillation Processes -- 8.1.1 Feasible Temperatures -- 8.1.2 Feasible Pressures -- 8.1.3 Feasible Dimensions of Columns -- 8.2 Fractionation of Binary Mixtures -- 8.2.1 Recycling of Diluted Sulfuric Acid -- 8.2.2 Ammonia Recovery from Wastewater -- 8.2.3 Hydrogen Chloride Recovery from Inert Gases -- 8.2.4 Linde Process for Air Separation -- 8.2.5 Process Water Purification -- 8.2.6 Steam Distillation -- 8.3 Fractionation of Multicomponent Zeotropic Mixtures -- 8.3.1 Separation Paths -- 8.3.2 Processes with Side Columns -- 8.4 Fractionation of Heterogeneous Azeotropic Mixtures -- 8.5 Fractionation of Azeotropic Mixtures by Pressure Swing Processes -- 8.6 Fractionation of Azeotropic Mixtures by Addition of an Entrainer -- 8.6.1 Processes for Systems Without Distillation Boundary -- 8.6.2 Processes for Systems with Distillation Boundary -- 8.6.3 Hybrid Processes -- 8.7 Industrial Processes of Reactive Distillation -- 8.7.1 Synthesis of MTBE -- 8.7.2 Synthesis of Mono-ethylene Glycol -- 8.7.3 Synthesis of TAME -- 8.7.4 Synthesis of Methyl Acetate -- 9 Design of Mass Transfer Equipment -- 9.1 Types of Design -- 9.1.1 Tray Columns -- 9.1.2 Packed Columns -- 9.1.3 Criteria for Use of Tray or Packed Columns -- 9.2 Design of Tray Columns.; 9.2.1 Design Parameters of Tray Columns -- 9.2.2 Operating Region of Tray Columns -- 9.2.3 Two-Phase Flow on Trays -- 9.2.4 Mass Transfer in the Two-Phase Layer on Column Trays -- 9.3 Design of Packed Columns -- 9.3.1 Design Parameters of Packed Columns -- 9.3.2 Operating Region of Packed Columns -- 9.3.3 Two-Phase Flow in Packed Columns -- 9.3.4 Mass Transfer in Packed Columns -- 9.A Appendix: Pressure Drop in Packed Beds -- 10 Control of Distillation Processes -- 10.1 Control Loops -- 10.1.1 Single Control Loop -- 10.1.2 Ratio Control Loop -- 10.1.3 Disturbance Feedforward Control Loop -- 10.1.4 Cascade Control Loop -- 10.2 Single Control Tasks for Distillation Columns -- 10.2.1 Liquid Level Control -- 10.2.2 Split Stream Control -- 10.2.3 Pressure Control -- 10.2.4 Product Concentration Control -- 10.3 Basic Control Configurations of Distillation Columns -- 10.3.1 Basic Control Systems Without Composition Control -- 10.3.2 One-Point Composition Control Configurations -- 10.3.3 Two-Point Composition Control Configurations -- 10.4 Application Ranges of the Basic Control Configurations -- 10.4.1 Impact of Split Parameters According to Split Rule 2 -- 10.4.2 Sharp Separations of Ideal Mixtures with Constant Relative Volatility at Minimum Reflux and Boilup Ratio -- 10.4.3 Extended Application Ranges of the Basic Control Configurations -- 10.5 Examples for Control Configurations of Distillation Processes -- 10.5.1 Azeotropic Distillation Process by Pressure Change -- 10.5.2 ; Distillation Process for Air Separation -- 10.5.3 Distillation Process with a Main and a Side Colum -- 10.5.4 Azeotropic Distillation Process by Using an Entrainer -- 10.6 Control Configurations for Batch Distillation Processes -- Index -- EULA.