Mixing of Immiscible Liquids
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 EQUIPMENT
4.1 Agitated Tanks
4.2 Flow Mixers
4.3 'High Shear' Mixers
5 SYSTEM PHYSICAL PROPERTIES
5.1 Density
5.2 Viscosity
5.3 Interfacial Tension
6 STIRRED VESSELS
6.1 Design for Complete Dispersion
6.2 Prediction of Phase Inversion
6.3 Design for Mass Transfer
6.4 Design for Dispersed Phase Mixing
6.5 Hold-Up in Continuous Vessels
7 FLOW MIXERS
7.1 Design for Turbulent Conditions
7.2 Design for Laminar Conditions
TABLES
1 REYNOLDS NUMBER RANGES
FIGURES
1 STANDARD TANK CONFIGURATION
2 EXPERIMENTAL RELATIONSHIP BETWEEN MASS
TRANSFER COEFFICIENT AND POWER DENSITY
Mixing of Solid-Liquid Systems
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 TYPICAL APPLICATIONS
5 AGITATED VESSELS
5.1 Suspension of Heavier-than-Liquid Solids
5.1.1 Dispersion
5.1.2 Agitator Speed Correlation
5.2 Floating Solids
5.3 Mass Transfer
6 JET MIXING FOR SOLID LIQUID AGITATION
6.1 Flat Bottomed Vessel
6.2 Changes in the Shape of the Vessel Base
7 NOMENCLATURE
8 BIBLIOGRAPHY
APPENDICES
A WORKED EXAMPLE
TABLES
1 VALUES OF Po AND ZWIETERING CONSTANT "S"
FOR USE IN EQUATION 1
FIGURES
1 RECOMMENDED CONFIGURATION
2 RECOMMENDED CONFIGURATION FOR DRAW-DOWN OF FLOATING SOLIDS IN AGITATED VESSEL
3 ALTERNATIVE RECOMMENDED CONFIGURATION
FOR DRAW-DOWN OF FLOATING SOLIDS IN FOR
AGITATED VESSEL
4 JET MIXING FOR SOLIDS SUSPENSION
5 ESTIMATION OF S FROM KNOWN DATA
Batch Distillation
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 BACKGROUND TO THE DESIGN
4.1 General
4.2 Choice of batch/continuous operation
4.3 Boiling point curve and cut policy
4.4 Method of design
4.5 Scope of calculations required for design
5 SIMPLE BATCH DISTILLATION
6 FRACTIONAL BATCH DISTILLATION
6.1 General
6.2 Approximate methods
6.3 Rigorous design - use of a computer model
6.4 Other factors influencing the design
6.4.1 Occupation
6.4.2 Choice of Batch Rectification or Stripping
6.4.3 Batch size
6.4.4 Initial estimate of cut policy
6.4.5 Liquid Holdup
6.4.6 Total reflux operation and heating-up time
6.4.7 Column operating pressure
6.5 Optimum Design of the Batch Still
6.6 Special design problems
7 GENERAL ASPECTS OF EQUIPMENT DESIGN
7.1 Kettle reboilers
7.2 Column Internals
7.3 Condensers and reflux split boxes
8 PROCESS CONTROL AND INSTRUMENTATION IN
BATCH DISTILLATION
9 MECHANICAL DESIGN FEATURES
10 BIBLIOGRAPHY
APPENDICES
A McCABE - THIELE METHOD - TYPICAL EXAMPLE
Gas - Liquid Reactors
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 PRELIMINARY CONSIDERATIONS
4.1 Preliminary Equipment Selection
4.2 Equipment for Low Viscosity Liquids
4.3 Equipment for High Viscosity Liquids
5 REACTOR DESIGN
6 ESSENTIAL THEORY
6.1 Rate and Yield Determining Steps
6.2 Chemical and Physical Rates
6.3 Modification for Exothermic and Complex Reactions
6.4 Preliminary Selection of Reactor Type
7 EXPERIMENTAL DETERMINATION OF REGIME
7.1 Direct Measurement of Reaction Kinetics
7.2 Laboratory Gas-Liquid Reactor Experiments
8 EQUILIBRIUM AND DIFFUSIVITY DATA SOURCES
9 OVERALL EFFECTS
9.1 Liquid Flow Patterns
9.2 Scale of Mixing
9.3 Gas Flow Pattern : Mean Driving Force for Mass Transfer
9.4 Gas-Liquid Reactor Modeling
9.5 Heat Transfer
9.6 Materials of Construction
9.7 Foaming
10 FINAL CHOICE OF REACTOR TYPE
11 SCALE-UP AND SPECIFICATION OF GAS-LIQUID
REACTORS
11.1 Bubble Columns
11.2 Packed Columns
11.3 Trickle Beds
11.4 Plate or Tray Columns
11.5 Spray Columns
11.6 Wiped Film
11.7 Spinning Film Reactors
11.8 Stirred Vessels
11.9 Plunging Jet
11.10 Surface Aerator
11.11 Static Mixers
11.12 Ejectors, Venturis and Orifice Plates
11.13 3-Phase Fluidized Bed
12 BIBLIOGRAPHY
TABLES
1 REGIMES OF GAS-LIQUID MASS TRANSFER WITH ISOTHERMAL CHEMICAL REACTION
2 REGIMES OF GAS-LIQUID MASS TRANSFER IGNORING LARGE EXOTHERMS OR OTHER COMPLICATIONS
3 COMPARATIVE MASS TRANSFER PERFORMANCE OF CONTACTING DEVICES
4 COMPARATIVE MASS TRANSFER DATA
5 CHOICE OF GAS-LIQUID REACTOR TYPE
FIGURES
1 RATE AND YIELD DETERMINING STEPS
2 ENHANCEMENT FACTOR vs HATTA NUMBER
3 ENHANCEMENT FACTOR vs HATTA NUMBER : EFFECT OF THERMAL & OTHER FACTORS
4 REACTORS FOR LIQUID-PHASE KINETICS
MEASUREMENT
5 EXPERIMENTS TO DETERMINE THE OPERATING
REGIME
6 EXPERIMENTS DETERMINE THE OPERATING REGIME WHERE A SOLID CATALYST IS INVOLVED
7 THE MIXED ZONES IN LOOPS' MODEL FOR STIRRED REACTORS
Solid Catalyzed Reactions
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 GENERAL BACKGROUND
4.1 General Considerations
5 SOLID CATALYZED GAS REACTIONS
5.1 Reaction Kinetics
5.2 Tests for Transport Limitations
5.3 Building a Reaction Kinetic Equation
6 INTRAPARTICLE
6.1 Types of Pore System
6.2 The Catalyst Effectiveness Factor
6.3 The Measurement of Effective Diffusivity
7 ENHANCEMENT OF INTRAPARTICLE
8 NOMENCLATURE
8.1 Dimensionless Parameters
8.2 Greek Letters
8.3 Subscripts
9 BIBLIOGRAPHY
9.1 Further Reading
APPENDICES
A LANGMUIR - HINSHELWOOD KINETICS
FIGURES
1 EFFECTIVE RATE CONSTANT
2 ITERATIVE APPROACH TO REACTOR MODEL
DEVELOPMENT
3 COMMON LABORATORY MICROREACTORS (FLOW TYPE)
4 THE BERTY REACTOR
5 STEPS IN BUILDING A REACTION RATE EQUATION
6 A CENTRAL-COMPOSITE DESIGN FOR TWO FACTORS
7 FIRST ORDER ISOTHERMAL IRREVERSIBLE
REACTION WITHIN A CATALYST SPHERE
8 INTEGRAL YIELD vs CONVERSION SHOWING EFFECT OF PELLET DIFFUSION
9 PREDICTED AND EXPERIMENTAL EFFECTIVENESS FACTORS
10 STRUCTURAL PERMEABILITY vs PRESSURE PARAMETER Z FOR BI-MODAL SUPPORTS
11 EFFECTIVENESS FACTOR vs THIELE MODULUS AND INTRAPARTICLE PECLET NUMBER
12 RELATIVE INCREASE IN CATALYST PERFORMANCE
The Selective Oxidation of n-Butane to Maleic Anhydride in a Catalyst Packed ...Gerard B. Hawkins
The Selective Oxidation of n-Butane to Maleic Anhydride in a Catalyst Packed Tubular Reactor
CONTENTS
0 INTRODUCTION
1 n-BUTANE OXIDATION
2 REACTION KINETICS
3 HEAT AND MASS TRANSFER PARAMETERS
4 NON-ISOTHERMAL, NON-ADIABATIC REACTOR MODELING
5 USE OF THE REACTOR MODEL IN OPERABILITY AND DESIGN STUDIES
6 BIBLIOGRAPHY
7 NOMENCLATURE
Study 1: Concept Hazard Review
CONTENTS
1.0 PURPOSE
1.0.1 Team
1.0.2 Timing
1.0.3 Preparation
1.0.4 Documentation
HAZARD STUDY 1: APPLICATION
1.1 Project Definition
1.2 Process Description
1.3 Materials Hazards
1.4 External Authorities
1.5 Organization and Human Factors
1.6 Additional Activities to be Completed
1.7 Review of Hazard Study 1
APPENDICES
A Chemical Hazard Guide Diagram
B Safety Risk Criteria - Limit Values for Tolerable Risk
C List of Additional Assessments
Shortcut Methods of Distillation Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 ESTIMATIONOF PLATEAGE AND REFLUX
REQUIREMENTS
2.1 Generalized Procedure for Nmin and Rmin
2.2 Equation based Procedure for Nmin and Rmin
3 PREDICTION OF OVERALL PLATE EFFICIENCY
4 SIZING OF MAIN PLANT ITEMS
4.1 Column Diameter
4.2 Surface Area of Condensers and Reboilers
FIGURES
1 NON-IDEAL EQUILIBRIUM CURVE
2 AT A GLANCE CHART BASED ON FENSKE,
UNDERWOOD
3 PLATE EFFICIENCY CORRELATION OF O’CONNEL
Mixing of Solid-Liquid Systems
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 TYPICAL APPLICATIONS
5 AGITATED VESSELS
5.1 Suspension of Heavier-than-Liquid Solids
5.1.1 Dispersion
5.1.2 Agitator Speed Correlation
5.2 Floating Solids
5.3 Mass Transfer
6 JET MIXING FOR SOLID LIQUID AGITATION
6.1 Flat Bottomed Vessel
6.2 Changes in the Shape of the Vessel Base
7 NOMENCLATURE
8 BIBLIOGRAPHY
APPENDICES
A WORKED EXAMPLE
TABLES
1 VALUES OF Po AND ZWIETERING CONSTANT "S"
FOR USE IN EQUATION 1
FIGURES
1 RECOMMENDED CONFIGURATION
2 RECOMMENDED CONFIGURATION FOR DRAW-DOWN OF FLOATING SOLIDS IN AGITATED VESSEL
3 ALTERNATIVE RECOMMENDED CONFIGURATION
FOR DRAW-DOWN OF FLOATING SOLIDS IN FOR
AGITATED VESSEL
4 JET MIXING FOR SOLIDS SUSPENSION
5 ESTIMATION OF S FROM KNOWN DATA
Batch Distillation
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 BACKGROUND TO THE DESIGN
4.1 General
4.2 Choice of batch/continuous operation
4.3 Boiling point curve and cut policy
4.4 Method of design
4.5 Scope of calculations required for design
5 SIMPLE BATCH DISTILLATION
6 FRACTIONAL BATCH DISTILLATION
6.1 General
6.2 Approximate methods
6.3 Rigorous design - use of a computer model
6.4 Other factors influencing the design
6.4.1 Occupation
6.4.2 Choice of Batch Rectification or Stripping
6.4.3 Batch size
6.4.4 Initial estimate of cut policy
6.4.5 Liquid Holdup
6.4.6 Total reflux operation and heating-up time
6.4.7 Column operating pressure
6.5 Optimum Design of the Batch Still
6.6 Special design problems
7 GENERAL ASPECTS OF EQUIPMENT DESIGN
7.1 Kettle reboilers
7.2 Column Internals
7.3 Condensers and reflux split boxes
8 PROCESS CONTROL AND INSTRUMENTATION IN
BATCH DISTILLATION
9 MECHANICAL DESIGN FEATURES
10 BIBLIOGRAPHY
APPENDICES
A McCABE - THIELE METHOD - TYPICAL EXAMPLE
Gas - Liquid Reactors
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 PRELIMINARY CONSIDERATIONS
4.1 Preliminary Equipment Selection
4.2 Equipment for Low Viscosity Liquids
4.3 Equipment for High Viscosity Liquids
5 REACTOR DESIGN
6 ESSENTIAL THEORY
6.1 Rate and Yield Determining Steps
6.2 Chemical and Physical Rates
6.3 Modification for Exothermic and Complex Reactions
6.4 Preliminary Selection of Reactor Type
7 EXPERIMENTAL DETERMINATION OF REGIME
7.1 Direct Measurement of Reaction Kinetics
7.2 Laboratory Gas-Liquid Reactor Experiments
8 EQUILIBRIUM AND DIFFUSIVITY DATA SOURCES
9 OVERALL EFFECTS
9.1 Liquid Flow Patterns
9.2 Scale of Mixing
9.3 Gas Flow Pattern : Mean Driving Force for Mass Transfer
9.4 Gas-Liquid Reactor Modeling
9.5 Heat Transfer
9.6 Materials of Construction
9.7 Foaming
10 FINAL CHOICE OF REACTOR TYPE
11 SCALE-UP AND SPECIFICATION OF GAS-LIQUID
REACTORS
11.1 Bubble Columns
11.2 Packed Columns
11.3 Trickle Beds
11.4 Plate or Tray Columns
11.5 Spray Columns
11.6 Wiped Film
11.7 Spinning Film Reactors
11.8 Stirred Vessels
11.9 Plunging Jet
11.10 Surface Aerator
11.11 Static Mixers
11.12 Ejectors, Venturis and Orifice Plates
11.13 3-Phase Fluidized Bed
12 BIBLIOGRAPHY
TABLES
1 REGIMES OF GAS-LIQUID MASS TRANSFER WITH ISOTHERMAL CHEMICAL REACTION
2 REGIMES OF GAS-LIQUID MASS TRANSFER IGNORING LARGE EXOTHERMS OR OTHER COMPLICATIONS
3 COMPARATIVE MASS TRANSFER PERFORMANCE OF CONTACTING DEVICES
4 COMPARATIVE MASS TRANSFER DATA
5 CHOICE OF GAS-LIQUID REACTOR TYPE
FIGURES
1 RATE AND YIELD DETERMINING STEPS
2 ENHANCEMENT FACTOR vs HATTA NUMBER
3 ENHANCEMENT FACTOR vs HATTA NUMBER : EFFECT OF THERMAL & OTHER FACTORS
4 REACTORS FOR LIQUID-PHASE KINETICS
MEASUREMENT
5 EXPERIMENTS TO DETERMINE THE OPERATING
REGIME
6 EXPERIMENTS DETERMINE THE OPERATING REGIME WHERE A SOLID CATALYST IS INVOLVED
7 THE MIXED ZONES IN LOOPS' MODEL FOR STIRRED REACTORS
Solid Catalyzed Reactions
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 GENERAL BACKGROUND
4.1 General Considerations
5 SOLID CATALYZED GAS REACTIONS
5.1 Reaction Kinetics
5.2 Tests for Transport Limitations
5.3 Building a Reaction Kinetic Equation
6 INTRAPARTICLE
6.1 Types of Pore System
6.2 The Catalyst Effectiveness Factor
6.3 The Measurement of Effective Diffusivity
7 ENHANCEMENT OF INTRAPARTICLE
8 NOMENCLATURE
8.1 Dimensionless Parameters
8.2 Greek Letters
8.3 Subscripts
9 BIBLIOGRAPHY
9.1 Further Reading
APPENDICES
A LANGMUIR - HINSHELWOOD KINETICS
FIGURES
1 EFFECTIVE RATE CONSTANT
2 ITERATIVE APPROACH TO REACTOR MODEL
DEVELOPMENT
3 COMMON LABORATORY MICROREACTORS (FLOW TYPE)
4 THE BERTY REACTOR
5 STEPS IN BUILDING A REACTION RATE EQUATION
6 A CENTRAL-COMPOSITE DESIGN FOR TWO FACTORS
7 FIRST ORDER ISOTHERMAL IRREVERSIBLE
REACTION WITHIN A CATALYST SPHERE
8 INTEGRAL YIELD vs CONVERSION SHOWING EFFECT OF PELLET DIFFUSION
9 PREDICTED AND EXPERIMENTAL EFFECTIVENESS FACTORS
10 STRUCTURAL PERMEABILITY vs PRESSURE PARAMETER Z FOR BI-MODAL SUPPORTS
11 EFFECTIVENESS FACTOR vs THIELE MODULUS AND INTRAPARTICLE PECLET NUMBER
12 RELATIVE INCREASE IN CATALYST PERFORMANCE
The Selective Oxidation of n-Butane to Maleic Anhydride in a Catalyst Packed ...Gerard B. Hawkins
The Selective Oxidation of n-Butane to Maleic Anhydride in a Catalyst Packed Tubular Reactor
CONTENTS
0 INTRODUCTION
1 n-BUTANE OXIDATION
2 REACTION KINETICS
3 HEAT AND MASS TRANSFER PARAMETERS
4 NON-ISOTHERMAL, NON-ADIABATIC REACTOR MODELING
5 USE OF THE REACTOR MODEL IN OPERABILITY AND DESIGN STUDIES
6 BIBLIOGRAPHY
7 NOMENCLATURE
Study 1: Concept Hazard Review
CONTENTS
1.0 PURPOSE
1.0.1 Team
1.0.2 Timing
1.0.3 Preparation
1.0.4 Documentation
HAZARD STUDY 1: APPLICATION
1.1 Project Definition
1.2 Process Description
1.3 Materials Hazards
1.4 External Authorities
1.5 Organization and Human Factors
1.6 Additional Activities to be Completed
1.7 Review of Hazard Study 1
APPENDICES
A Chemical Hazard Guide Diagram
B Safety Risk Criteria - Limit Values for Tolerable Risk
C List of Additional Assessments
Shortcut Methods of Distillation Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 ESTIMATIONOF PLATEAGE AND REFLUX
REQUIREMENTS
2.1 Generalized Procedure for Nmin and Rmin
2.2 Equation based Procedure for Nmin and Rmin
3 PREDICTION OF OVERALL PLATE EFFICIENCY
4 SIZING OF MAIN PLANT ITEMS
4.1 Column Diameter
4.2 Surface Area of Condensers and Reboilers
FIGURES
1 NON-IDEAL EQUILIBRIUM CURVE
2 AT A GLANCE CHART BASED ON FENSKE,
UNDERWOOD
3 PLATE EFFICIENCY CORRELATION OF O’CONNEL
Troubleshooting in Distillation Columns
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 FLOW DIAGRAM FOR TROUBLESHOOTING
5 GENERAL APPRAISAL OF PROBLEM
5.1 Is the Problem Real?
5.2 What Is the Magnitude of the Problem?
5.3 Is it the Column or the Associated Equipment which is Causing the Problem?
6 PROBLEMS IN THE COLUMN
6.1 Capacity Problems
6.2 Efficiency Problems
7 PROBLEMS OUTSIDE THE COLUMN
7.1 Effect of Other Units on Column Performance
7.2 Column Control System
7.3 Improper Operating Conditions
7.4 Auxiliary Equipment
8 USEFUL BACKGROUND READING
9 BIBLIOGRAPHY
FIGURES
1 FLOW DIAGRAM FOR TROUBLESHOOTING
2 DETERMINATION OF COLUMN CAPACITY
Reactor Arrangement for Continuous Vapor Phase ChlorinationGerard B. Hawkins
Reactor Arrangement for Continuous Vapor Phase Chlorination
CONTENTS
1 BACKGROUND
2 REACTOR
3 CHEMICAL SYSTEM
4 PROCESS CHEMISTRY
5 KINETICS EXPERIMENTS AND MODELING
6 INTERPRETATION OF KINETICS INFORMATION
7 OPERATING CONDITIONS AND REACTOR DESIGN
8 REACTOR STABILITY AND CONTROL
FIGURES
1 POSTULATED REACTION PATHS FOR PROGRESSIVE CHLORINATION OF B-PICOLINE 3
2 CHLORINATION OF b-PICOLINE: MODEL PREDICTIONS OF PRODUCT DISTRIBUTION IN FULLY-MIXED REACTOR
3 TWO-STAGE REACTOR: RATE OF CHLORINATION OF b-PICOLINE
DOCUMENTS REFERRED TO IN THIS PROCESS ENGINEERING GUIDE
How to Use the GBHE Mixing Guides
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 THE MIXING GUIDES
4.1 Mixing Guides
4.2 GBHE Mixing and Agitation Manual
5 DEVICE SELECTION
6 MIXING QUESTIONNAIRE
6.1 What is being mixed?
6.2 Why is it being mixed?
6.3 How is it to be mixed?
6.4 Is Heat Transfer Important?
6.5 Is Mixing Time Important?
6.6 Is Inventory Important?
6.7 Is Subsequent Phase Separation Important?
6.8 What Quantities?
6.9 What are the Selection Criteria?
6.10 What Data are required?
7 BASICS
7.1 Bulk Movement
7.2 Shear and Elongation
7.3 Turbulent Diffusion
7.4 Molecular Diffusion
7.5 Mixing Mechanisms
APPENDICES
A ROTATING MIXING DEVICES
B MIXING DEVICES WITHOUT MOVING PARTS
How to use the GBHE Reactor Technology Guides
0 INTRODUCTION / PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 BACKGROUND
5 THE DECISION TREE
6 GBHE REACTION ENGINEERING
7 GENERAL ASPECTS OF REACTOR TECHNOLOGY
7.1 Criteria of Reactor Performance
7.2 Factors of Economic Importance
7.3 Physicochemical Mechanisms
8 GENERAL GUIDE TO SELECTION OF REACTOR TYPE AND OPERATION
8.1 Choice of Reactor Type
8.2 Reaction Mechanism and Kinetics
8.3 Thermodynamics
8.4 Other Factors
9 GENERAL REFERENCES AND SOURCES OF
INFORMATION
APPENDICES
A RELATIONSHIP BEWTEEN DEFINED TERMS
FIGURES
1 DECISION TREE
2 RELATIVE YIELDS OF B FOR BATCH (OR PLUG FLOW) AND CST REACTORS
3 REACTOR SURVEY FORM
"SEDIMENTATION"
INTRODUCTION - THE PHENOMENON OF SEDIMENTATION
Sedimentation is the physical process whereby solid particles, of greater density than their suspending medium, will tend to separate into regions of higher concentration under the influence of gravity. As a solids/liquids separation technique it therefore possesses the great advantage of utilizing a natural, and therefore costless, driving force. This section of the suspension processing Guide is Intended to provide an Introduction to the science of the subject, and the means to judge where and how best to exploit sedimentation as a separation (or other processing) technique.
As a scientific discipline the subject of sedimentation is vast with perspectives ranging from the field of chemical engineering through to theoretical physics being covered In the literature [1-11]. Good reviews of the subject, with a bias towards the engineering aspects, have been written by Fitch and Koz [12, 13]. A short summary of some of the more relevant contributions from the literature is also provided in GBHE-SPG-PEG-302 “Basic Principles & Test Methods”, of the Suspensions Processing Guides.
.
The sedimentation process is traditionally divided into ..."
Design and Simulation of Continuous Distillation ColumnsGerard B. Hawkins
Design and Simulation of Continuous Distillation Columns
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 FRACTIONAL DISTILLATION
5 ROUGH METHOD OF COLUMN DESIGN
5.1 Sharp Separations
5.2 Sloppy Separations
6 DETAIL DESIGN USING THE CHEMCAD DISTILLATION PROGRAM
6.1 Sharp Separations
6.2 Sloppy Separations
7 COMPLEX COLUMNS
7.1 Multiple Feeds
7.2 Sidestream Take-Offs
8 DESIGN USING A LABORATORY COLUMN
SIMULATION
9 DESIGN USING ACTUAL PLANT DATA
9.1 Uprating or Debottlenecking Exercises
10 REFERENCES
APPENDICES
A WORKED EXAMPLE
B SLOPPY SEPARATIONS
C SIMULATION USING PLANT DATA : CASE HISTORIES
TABLES
Mixing of Miscible Liquids
Mixing of Miscible Liquids
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 SELECTION OF EQUIPMENT
4.1 Mechanically Agitated Vessels
4.2 Jet Mixed Vessels
4.3 Tubular ('Flow') Mixers
5 AGITATED VESSELS
5.1 Mixing Time for Liquids in Stirred Tanks
5.2 Power Requirements
5.3 Vortex Formation and Surface Entrainment in Unbaffled and Baffled Vessels
5.4 Heat-Transfer in Stirred Vessels
5.5 Flow and Circulation
6 JET MIXED TANKS
6.1 Introduction
6.2 Recommended Configuration
6.3 Design Procedure
6.4 Design for Continuous Mixing
7 TUBULAR JET FLOW MIXERS FOR MISCIBLE LIQUIDS
7.1 Recommended Configurations
7.2 Mixer Design
7.3 Additional Considerations
8 MOTIONLESS MIXERS
8.1 Recommended Types
8.2 Correlations
TABLES
1 TYPICAL CONSTANTS FOR EQUATION (1)
2 POWER CURVES FIGURES AND CORRECTION FACTORS
3 VORTEX PARAMETERS, TURBINE, PROPELLER AND SAWTOOTH
4 CHARGING A HOT VESSEL WITH A COLD PRODUCT
5 INJECTING A HOT FLUID INTO THE JACKET OF A COLD VESSEL
6 TYPICAL DISCHARGE COEFFICIENTS
7 CONSTRAINTS FOR LAMINAR FLOW MOTIONLESS MIXERS
8 CONSTANTS FOR TURBULENT FLOW MOTIONLESS MIXERS
9 LENGTH FACTORS FOR HIGH VISCOSITY RATIOS
FIGURES
1 POWER NUMBERS FOR 45° ANGLED-BLADE TURBINES
2 CORRECTION FACTORS FOR DIAMETER RATIOS
3 BLADE ANGLE AND THICKNESS CORRECTION FACTORS
4 POWER NUMBERS FOR SINGLE 60° ANGLED-BLADE TURBINES
5 POWER NUMBERS FOR TWIN 60° ANGLED-BLADE TURBINES
6 POWER NUMBERS FOR TRIPLE 60° ANGLED-BLADE TURBINES
7 BAFFLE WIDTH AND NUMBER CORRECTION FACTORS FOR DIFFERENT DIAMETER RATIOS
8 CORRECTION FACTORS FOR SUBMERGENCE
9 CORRECTION FACTORS FOR SEPARATION
10 POWER NUMBERS FOR DISC-TURBINES
11 CORRECTION FACTORS FOR BAFFLES
12 CORRECTION FACTORS FOR BASE CLEARANCE
13 CORRECTION FACTORS FOR SUBMERGENCE
14 POWER NUMBERS FOR RETREAT-CURVE IMPELLERS
15 CORRECTION FACTORS FOR PARTIAL BAFFLES
16 POWER NUMBERS CORRECTION FACTORS FOR RETREAT-CURVE AND IMPELLERS H/T RATIOS OF 2.0
17 POWER NUMBERS FOR FLAT-BLADED TURBINES
18 BOTTOM CLEARANCE CORRECTION FACTOR
19 POWER NUMBERS FOR ANCHOR AND GATE AGITATORS
20 POWER NUMBERS FOR PROPELLERS
21 IMPELLER SPACING CORRECTION FACTORS
22 STANDARD NOTATION FOR VORTEX CALCULATIONS
23 VORTEX DATA FOR 2 - BLADED PADDLES
(W/D = 0.33, T/D = 2)
24 VORTEX CORRECTION FACTORS FOR PADDLES
25 JET DIRECTION
26 SINGLE JET MIXERS
27 MULTIJET MIXERS
28 SERIES ARRANGEMENT OF MIXERS
29 BATCH MIXERS
30 DESIGN PROCEDURE
31 EMPIRICAL FACTORS
32 RECIRCULATION ZONES
33 FRICTION FACTOR DATA FOR KENICS AND SULZER MIXERS
Tools for Reactor Modeling:
THE ELEMENT POTENTIAL METHOD FOR CHEMICAL EQUILIBRIUM ANALYSIS: STANJAN
CONTENTS
1 SCOPE
2 SUMMARY
3 INTRODUCTION
4 EXAMPLES
4.1 CARBON-RICH C-0 SYSTEM
4.2 EXAMPLE WITH TWO COMPLEX PHASES
4.3 GAS TURBINE ENGINE EXAMPLE
4.4 OTHER APPLICATIONS
APPENDIX
FIGURES
5.1 EXAMPLE RUN LOG FOR CARBON-RICH C-O SYSTEM
5.2 OUTPUT FOR EXAMPLE WITH TWO COMPLEX PHASES
5.3 FIRST STEP IN THE TURBINE EXAMPLE: CALCULATION OF THE ENTHALPY OF THE REACTANTS
5.4 SECOND STEP IN THE TURBINE EXAMPLE: CALCULATION OF THE ADIABATIC FLAME TEMPERATURE
5.5 THIRD STEP IN THE TURBINE EXAMPLE: CALCULATION OF THE NOZZLE EXIT STATE
AVAILABILITY AND IMPLEMENTATION OF STANJAN
REFERENCES
Fixed Bed Reactor Scale-up Checklist
The purpose of this checklist is to identify the stages and potential problems associated with the scale up of fixed bed reactors from the drawing board to the full scale plant, and to determine how they should be checked.
The checking can be done using various methods. These are:
• Literature data.
• Lab testing.
• Calculation.
• Modeling.
• Semi-tech testing.
• Piloting or Sidestream testing.
Identifying the stages that need to be addressed for a particular catalyst/reactor development will help in estimating the time needed for the development of the reactor
BENFIELD LIQUOR:Determination of Diethanolamine Using an Auto TitratorGerard B. Hawkins
BENFIELD LIQUOR:Determination of Diethanolamine Using an Auto Titrator
1 SCOPE AND FIELD OF APPLICATION
This method is suitable for the determination of diethanolamine in Benfield Liquor.
2 PRINCIPLE
Diethanolamine is converted quantitatively into ammonia by boiling in the presence of sulfuric acid and copper sulfate. The ammonia is distilled from an alkaline medium and absorbed into boric acid. The solution is titrated with standard acid.
GE / Texaco Gasifier Feed to a Lurgi Methanol Plant and its Effect on Methano...Gerard B. Hawkins
GE / Texaco Gasifier Feed to a Lurgi Methanol Plant and its Effect on Methanol Production
CONTENTS
0 Methanol Synthesis Introduction
1 Executive Summary
2 Design Basis
2.1.1 Train I Design Basis
2.1.2 Train II Design Basis
2.1.3 Train III Design Basis
2.2 Design Philosophy
2.2.1 Operability Review
2.3 Assumptions
2.4 Train IV Flowsheet
2.4.1 CO2 Removal
3 Discussion
3.1 Natural Gas Consumption Figures
3.1.1 Base Case
3.1.2 Case 1 – Coal Gasification in Service
3.1.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.2 Methanol Production Figures
3.2.1 Base Case
3.2.2 Case 1 – Coal Gasification in Service
3.2.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.3 85% Natural Gas Availability
3.4 100% Natural Gas Availability
3.5 CO2 Emissions
3.5.1 Base Case
3.5.2 Case 1 – Coal Gasification in Service
3.5.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.6 Specific Consumption Figures
3.6.1 Base Case
3.6.2 Case 1 – Coal Gasification and CO2 Import
3.6.3 Case 2 – Coal Gasification and No CO2 Import
3.7 Train IV Synthesis Gas Composition
4 Further Work
5 Conclusion
APPENDIX
Important Stream Data – Material Balance Stream Data
Texaco Gasifier with HP Steam Raising Boiler
CHARACTERISTICS OF COAL
Material Balance Considerations
Reactor and Catalyst Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 CATALYST DESIGN
4.1 Equivalent Pellet Diameter
4.2 Voidage
4.3 Pellet Density
5 REACTOR DESIGN
6 CATALYST SUPPORT
6.1 Choice of Support
TABLES
1 CATALYST SUPPORT SHAPES
2 SECONDARY REFORMER SPREADSHEET
FIGURES
1 GRAPH OF EFFECTIVENESS v THIELE MODULUS
2 VARIATION OF COSTS WITH CATALYST SIZE
3 VARIATION OF COSTS WITH CATALYST BED VOIDAGE
4 VARIATION OF COSTS WITH VESSEL DIAMETER
Graphical Representation of Liquid-Liquid Phase EquilibriaGerard B. Hawkins
Graphical Representation of
Liquid-Liquid Phase Equilibria
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 GRAPHICAL REPRESENTATIONS OF PHYSICAL
PROPERTIES
4.1 Use of Composition Diagrams
4.2 Ternary Systems with Immiscible Liquids
4.3 Graphical Design Using Ternary Diagrams
APPENDICES
A INTERPOLATION AND CORRELATION OF THE LINES
FIGURES
1 TRIANGULAR CO-ORDINATES
2 TYPE 1 SYSTEM: ONE PAIR OF PARTIALLY MISCIBLE LIQUIDS
3 TYPE 2 SYSTEM: TWO PAIR OF PARTIALLYMISCIBLE LIQUIDS
4 DESIGN OF COUNTERCURRENT EXTRACTION SYSTEM WITHOUT REFLUX – TYPE 1 SYSTEM
5 BLOCK DIAGRAM OF REFLUXED LIQUID-LIQUID EXTRACTION
6 DESIGN OF COUNTERCURRENT SYSTEM WITH REFLUX
7 CONSTRUCTION OF THE CONJUGATE LINE
Mass transfer studies in an agitated vessel with radial axial impeller combin...eSAT Journals
Abstract The effect of radial-axial impeller combination in dual configuration was tested for gas liquid mass transfer coefficient (KLa) and compared with that of dual axial impeller (30º Pitched blade) combination. The trials were conducted at gas rates of 2litre/min to 10litre/min and agitation rates of 180rpm to 360rpm.Good mass transfer coefficient was obtained by replacing the lower axial impeller with a radial impeller. Rushton Turbine and Curved blade (half pipe) impeller were used in replacing the lower axial impeller. Amongst the two radial impellers, curved blade resulted in higher KLa than Rushton Turbine at highest gassing rate tested. About 15-35% and 20-48% increase in KLa was observed by replacing lower pitched blade impeller with Rushton and Curved blade impeller each. The results from the present study shows the capability of replacing lower axial impeller with Radial impeller and retrofitting existing lower Rushton Turbine with Curved blade impeller. Keywords: Mass transfer coefficient, Rushton, Axial, agitated vessel.
Troubleshooting in Distillation Columns
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 FLOW DIAGRAM FOR TROUBLESHOOTING
5 GENERAL APPRAISAL OF PROBLEM
5.1 Is the Problem Real?
5.2 What Is the Magnitude of the Problem?
5.3 Is it the Column or the Associated Equipment which is Causing the Problem?
6 PROBLEMS IN THE COLUMN
6.1 Capacity Problems
6.2 Efficiency Problems
7 PROBLEMS OUTSIDE THE COLUMN
7.1 Effect of Other Units on Column Performance
7.2 Column Control System
7.3 Improper Operating Conditions
7.4 Auxiliary Equipment
8 USEFUL BACKGROUND READING
9 BIBLIOGRAPHY
FIGURES
1 FLOW DIAGRAM FOR TROUBLESHOOTING
2 DETERMINATION OF COLUMN CAPACITY
Reactor Arrangement for Continuous Vapor Phase ChlorinationGerard B. Hawkins
Reactor Arrangement for Continuous Vapor Phase Chlorination
CONTENTS
1 BACKGROUND
2 REACTOR
3 CHEMICAL SYSTEM
4 PROCESS CHEMISTRY
5 KINETICS EXPERIMENTS AND MODELING
6 INTERPRETATION OF KINETICS INFORMATION
7 OPERATING CONDITIONS AND REACTOR DESIGN
8 REACTOR STABILITY AND CONTROL
FIGURES
1 POSTULATED REACTION PATHS FOR PROGRESSIVE CHLORINATION OF B-PICOLINE 3
2 CHLORINATION OF b-PICOLINE: MODEL PREDICTIONS OF PRODUCT DISTRIBUTION IN FULLY-MIXED REACTOR
3 TWO-STAGE REACTOR: RATE OF CHLORINATION OF b-PICOLINE
DOCUMENTS REFERRED TO IN THIS PROCESS ENGINEERING GUIDE
How to Use the GBHE Mixing Guides
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 THE MIXING GUIDES
4.1 Mixing Guides
4.2 GBHE Mixing and Agitation Manual
5 DEVICE SELECTION
6 MIXING QUESTIONNAIRE
6.1 What is being mixed?
6.2 Why is it being mixed?
6.3 How is it to be mixed?
6.4 Is Heat Transfer Important?
6.5 Is Mixing Time Important?
6.6 Is Inventory Important?
6.7 Is Subsequent Phase Separation Important?
6.8 What Quantities?
6.9 What are the Selection Criteria?
6.10 What Data are required?
7 BASICS
7.1 Bulk Movement
7.2 Shear and Elongation
7.3 Turbulent Diffusion
7.4 Molecular Diffusion
7.5 Mixing Mechanisms
APPENDICES
A ROTATING MIXING DEVICES
B MIXING DEVICES WITHOUT MOVING PARTS
How to use the GBHE Reactor Technology Guides
0 INTRODUCTION / PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 BACKGROUND
5 THE DECISION TREE
6 GBHE REACTION ENGINEERING
7 GENERAL ASPECTS OF REACTOR TECHNOLOGY
7.1 Criteria of Reactor Performance
7.2 Factors of Economic Importance
7.3 Physicochemical Mechanisms
8 GENERAL GUIDE TO SELECTION OF REACTOR TYPE AND OPERATION
8.1 Choice of Reactor Type
8.2 Reaction Mechanism and Kinetics
8.3 Thermodynamics
8.4 Other Factors
9 GENERAL REFERENCES AND SOURCES OF
INFORMATION
APPENDICES
A RELATIONSHIP BEWTEEN DEFINED TERMS
FIGURES
1 DECISION TREE
2 RELATIVE YIELDS OF B FOR BATCH (OR PLUG FLOW) AND CST REACTORS
3 REACTOR SURVEY FORM
"SEDIMENTATION"
INTRODUCTION - THE PHENOMENON OF SEDIMENTATION
Sedimentation is the physical process whereby solid particles, of greater density than their suspending medium, will tend to separate into regions of higher concentration under the influence of gravity. As a solids/liquids separation technique it therefore possesses the great advantage of utilizing a natural, and therefore costless, driving force. This section of the suspension processing Guide is Intended to provide an Introduction to the science of the subject, and the means to judge where and how best to exploit sedimentation as a separation (or other processing) technique.
As a scientific discipline the subject of sedimentation is vast with perspectives ranging from the field of chemical engineering through to theoretical physics being covered In the literature [1-11]. Good reviews of the subject, with a bias towards the engineering aspects, have been written by Fitch and Koz [12, 13]. A short summary of some of the more relevant contributions from the literature is also provided in GBHE-SPG-PEG-302 “Basic Principles & Test Methods”, of the Suspensions Processing Guides.
.
The sedimentation process is traditionally divided into ..."
Design and Simulation of Continuous Distillation ColumnsGerard B. Hawkins
Design and Simulation of Continuous Distillation Columns
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 FRACTIONAL DISTILLATION
5 ROUGH METHOD OF COLUMN DESIGN
5.1 Sharp Separations
5.2 Sloppy Separations
6 DETAIL DESIGN USING THE CHEMCAD DISTILLATION PROGRAM
6.1 Sharp Separations
6.2 Sloppy Separations
7 COMPLEX COLUMNS
7.1 Multiple Feeds
7.2 Sidestream Take-Offs
8 DESIGN USING A LABORATORY COLUMN
SIMULATION
9 DESIGN USING ACTUAL PLANT DATA
9.1 Uprating or Debottlenecking Exercises
10 REFERENCES
APPENDICES
A WORKED EXAMPLE
B SLOPPY SEPARATIONS
C SIMULATION USING PLANT DATA : CASE HISTORIES
TABLES
Mixing of Miscible Liquids
Mixing of Miscible Liquids
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 SELECTION OF EQUIPMENT
4.1 Mechanically Agitated Vessels
4.2 Jet Mixed Vessels
4.3 Tubular ('Flow') Mixers
5 AGITATED VESSELS
5.1 Mixing Time for Liquids in Stirred Tanks
5.2 Power Requirements
5.3 Vortex Formation and Surface Entrainment in Unbaffled and Baffled Vessels
5.4 Heat-Transfer in Stirred Vessels
5.5 Flow and Circulation
6 JET MIXED TANKS
6.1 Introduction
6.2 Recommended Configuration
6.3 Design Procedure
6.4 Design for Continuous Mixing
7 TUBULAR JET FLOW MIXERS FOR MISCIBLE LIQUIDS
7.1 Recommended Configurations
7.2 Mixer Design
7.3 Additional Considerations
8 MOTIONLESS MIXERS
8.1 Recommended Types
8.2 Correlations
TABLES
1 TYPICAL CONSTANTS FOR EQUATION (1)
2 POWER CURVES FIGURES AND CORRECTION FACTORS
3 VORTEX PARAMETERS, TURBINE, PROPELLER AND SAWTOOTH
4 CHARGING A HOT VESSEL WITH A COLD PRODUCT
5 INJECTING A HOT FLUID INTO THE JACKET OF A COLD VESSEL
6 TYPICAL DISCHARGE COEFFICIENTS
7 CONSTRAINTS FOR LAMINAR FLOW MOTIONLESS MIXERS
8 CONSTANTS FOR TURBULENT FLOW MOTIONLESS MIXERS
9 LENGTH FACTORS FOR HIGH VISCOSITY RATIOS
FIGURES
1 POWER NUMBERS FOR 45° ANGLED-BLADE TURBINES
2 CORRECTION FACTORS FOR DIAMETER RATIOS
3 BLADE ANGLE AND THICKNESS CORRECTION FACTORS
4 POWER NUMBERS FOR SINGLE 60° ANGLED-BLADE TURBINES
5 POWER NUMBERS FOR TWIN 60° ANGLED-BLADE TURBINES
6 POWER NUMBERS FOR TRIPLE 60° ANGLED-BLADE TURBINES
7 BAFFLE WIDTH AND NUMBER CORRECTION FACTORS FOR DIFFERENT DIAMETER RATIOS
8 CORRECTION FACTORS FOR SUBMERGENCE
9 CORRECTION FACTORS FOR SEPARATION
10 POWER NUMBERS FOR DISC-TURBINES
11 CORRECTION FACTORS FOR BAFFLES
12 CORRECTION FACTORS FOR BASE CLEARANCE
13 CORRECTION FACTORS FOR SUBMERGENCE
14 POWER NUMBERS FOR RETREAT-CURVE IMPELLERS
15 CORRECTION FACTORS FOR PARTIAL BAFFLES
16 POWER NUMBERS CORRECTION FACTORS FOR RETREAT-CURVE AND IMPELLERS H/T RATIOS OF 2.0
17 POWER NUMBERS FOR FLAT-BLADED TURBINES
18 BOTTOM CLEARANCE CORRECTION FACTOR
19 POWER NUMBERS FOR ANCHOR AND GATE AGITATORS
20 POWER NUMBERS FOR PROPELLERS
21 IMPELLER SPACING CORRECTION FACTORS
22 STANDARD NOTATION FOR VORTEX CALCULATIONS
23 VORTEX DATA FOR 2 - BLADED PADDLES
(W/D = 0.33, T/D = 2)
24 VORTEX CORRECTION FACTORS FOR PADDLES
25 JET DIRECTION
26 SINGLE JET MIXERS
27 MULTIJET MIXERS
28 SERIES ARRANGEMENT OF MIXERS
29 BATCH MIXERS
30 DESIGN PROCEDURE
31 EMPIRICAL FACTORS
32 RECIRCULATION ZONES
33 FRICTION FACTOR DATA FOR KENICS AND SULZER MIXERS
Tools for Reactor Modeling:
THE ELEMENT POTENTIAL METHOD FOR CHEMICAL EQUILIBRIUM ANALYSIS: STANJAN
CONTENTS
1 SCOPE
2 SUMMARY
3 INTRODUCTION
4 EXAMPLES
4.1 CARBON-RICH C-0 SYSTEM
4.2 EXAMPLE WITH TWO COMPLEX PHASES
4.3 GAS TURBINE ENGINE EXAMPLE
4.4 OTHER APPLICATIONS
APPENDIX
FIGURES
5.1 EXAMPLE RUN LOG FOR CARBON-RICH C-O SYSTEM
5.2 OUTPUT FOR EXAMPLE WITH TWO COMPLEX PHASES
5.3 FIRST STEP IN THE TURBINE EXAMPLE: CALCULATION OF THE ENTHALPY OF THE REACTANTS
5.4 SECOND STEP IN THE TURBINE EXAMPLE: CALCULATION OF THE ADIABATIC FLAME TEMPERATURE
5.5 THIRD STEP IN THE TURBINE EXAMPLE: CALCULATION OF THE NOZZLE EXIT STATE
AVAILABILITY AND IMPLEMENTATION OF STANJAN
REFERENCES
Fixed Bed Reactor Scale-up Checklist
The purpose of this checklist is to identify the stages and potential problems associated with the scale up of fixed bed reactors from the drawing board to the full scale plant, and to determine how they should be checked.
The checking can be done using various methods. These are:
• Literature data.
• Lab testing.
• Calculation.
• Modeling.
• Semi-tech testing.
• Piloting or Sidestream testing.
Identifying the stages that need to be addressed for a particular catalyst/reactor development will help in estimating the time needed for the development of the reactor
BENFIELD LIQUOR:Determination of Diethanolamine Using an Auto TitratorGerard B. Hawkins
BENFIELD LIQUOR:Determination of Diethanolamine Using an Auto Titrator
1 SCOPE AND FIELD OF APPLICATION
This method is suitable for the determination of diethanolamine in Benfield Liquor.
2 PRINCIPLE
Diethanolamine is converted quantitatively into ammonia by boiling in the presence of sulfuric acid and copper sulfate. The ammonia is distilled from an alkaline medium and absorbed into boric acid. The solution is titrated with standard acid.
GE / Texaco Gasifier Feed to a Lurgi Methanol Plant and its Effect on Methano...Gerard B. Hawkins
GE / Texaco Gasifier Feed to a Lurgi Methanol Plant and its Effect on Methanol Production
CONTENTS
0 Methanol Synthesis Introduction
1 Executive Summary
2 Design Basis
2.1.1 Train I Design Basis
2.1.2 Train II Design Basis
2.1.3 Train III Design Basis
2.2 Design Philosophy
2.2.1 Operability Review
2.3 Assumptions
2.4 Train IV Flowsheet
2.4.1 CO2 Removal
3 Discussion
3.1 Natural Gas Consumption Figures
3.1.1 Base Case
3.1.2 Case 1 – Coal Gasification in Service
3.1.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.2 Methanol Production Figures
3.2.1 Base Case
3.2.2 Case 1 – Coal Gasification in Service
3.2.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.3 85% Natural Gas Availability
3.4 100% Natural Gas Availability
3.5 CO2 Emissions
3.5.1 Base Case
3.5.2 Case 1 – Coal Gasification in Service
3.5.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.6 Specific Consumption Figures
3.6.1 Base Case
3.6.2 Case 1 – Coal Gasification and CO2 Import
3.6.3 Case 2 – Coal Gasification and No CO2 Import
3.7 Train IV Synthesis Gas Composition
4 Further Work
5 Conclusion
APPENDIX
Important Stream Data – Material Balance Stream Data
Texaco Gasifier with HP Steam Raising Boiler
CHARACTERISTICS OF COAL
Material Balance Considerations
Reactor and Catalyst Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 CATALYST DESIGN
4.1 Equivalent Pellet Diameter
4.2 Voidage
4.3 Pellet Density
5 REACTOR DESIGN
6 CATALYST SUPPORT
6.1 Choice of Support
TABLES
1 CATALYST SUPPORT SHAPES
2 SECONDARY REFORMER SPREADSHEET
FIGURES
1 GRAPH OF EFFECTIVENESS v THIELE MODULUS
2 VARIATION OF COSTS WITH CATALYST SIZE
3 VARIATION OF COSTS WITH CATALYST BED VOIDAGE
4 VARIATION OF COSTS WITH VESSEL DIAMETER
Graphical Representation of Liquid-Liquid Phase EquilibriaGerard B. Hawkins
Graphical Representation of
Liquid-Liquid Phase Equilibria
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 GRAPHICAL REPRESENTATIONS OF PHYSICAL
PROPERTIES
4.1 Use of Composition Diagrams
4.2 Ternary Systems with Immiscible Liquids
4.3 Graphical Design Using Ternary Diagrams
APPENDICES
A INTERPOLATION AND CORRELATION OF THE LINES
FIGURES
1 TRIANGULAR CO-ORDINATES
2 TYPE 1 SYSTEM: ONE PAIR OF PARTIALLY MISCIBLE LIQUIDS
3 TYPE 2 SYSTEM: TWO PAIR OF PARTIALLYMISCIBLE LIQUIDS
4 DESIGN OF COUNTERCURRENT EXTRACTION SYSTEM WITHOUT REFLUX – TYPE 1 SYSTEM
5 BLOCK DIAGRAM OF REFLUXED LIQUID-LIQUID EXTRACTION
6 DESIGN OF COUNTERCURRENT SYSTEM WITH REFLUX
7 CONSTRUCTION OF THE CONJUGATE LINE
Mass transfer studies in an agitated vessel with radial axial impeller combin...eSAT Journals
Abstract The effect of radial-axial impeller combination in dual configuration was tested for gas liquid mass transfer coefficient (KLa) and compared with that of dual axial impeller (30º Pitched blade) combination. The trials were conducted at gas rates of 2litre/min to 10litre/min and agitation rates of 180rpm to 360rpm.Good mass transfer coefficient was obtained by replacing the lower axial impeller with a radial impeller. Rushton Turbine and Curved blade (half pipe) impeller were used in replacing the lower axial impeller. Amongst the two radial impellers, curved blade resulted in higher KLa than Rushton Turbine at highest gassing rate tested. About 15-35% and 20-48% increase in KLa was observed by replacing lower pitched blade impeller with Rushton and Curved blade impeller each. The results from the present study shows the capability of replacing lower axial impeller with Radial impeller and retrofitting existing lower Rushton Turbine with Curved blade impeller. Keywords: Mass transfer coefficient, Rushton, Axial, agitated vessel.
Gas-Solid-Liquid Mixing Systems
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 SELECTION OF EQUIPMENT
5 THREE-PHASE MASS TRANSFER WITH CHEMICAL REACTION
6 STIRRED VESSEL DESIGN
6.1 Agitator Design
6.2 Design for Solids Suspension
6.3 Vessel Design
6.4 Gas-Liquid Mass Transfer Coefficient and Surface Area
7 THREE-PHASE FLUIDIZED BEDS
7.1 Gas and Liquid Hold-Up
7.2 Calculation Procedure
7.3 Bubble Size
7.4 Mass Transfer
7.5 Heat Transfer
7.6 Elutriation
8 SLURRY REACTORS
8.1 Gas Rate
8.2 Mass Transfer
9 NOMENCLATURE
10 BIBLIOGRAPHY
GAS DISPERSION - A Definitive Guide to Accidental Releases of Heavy GasesGerard B. Hawkins
GAS DISPERSION - A Definitive Guide to Accidental Releases of Heavy Gases
This Process Safety Guide has been written with the aim of assisting process engineers, hazard analysts and environmental advisers in carrying out gas dispersion calculations. The Guide aims to provide assistance by:
• Improving awareness of the range of dispersion models available within GBHE, and providing guidance in choosing the most appropriate model for a particular application.
• Providing guidance to ensure that source terms and other model inputs are correctly specified, and the models are used within their range of applicability.
• Providing guidance to deal with particular topics in gas dispersion such as dense gas dispersion, complex terrain, and modeling the chemistry of oxides of nitrogen.
• Providing general background on air quality and dispersion modeling issues such as meteorology and air quality standards.
• Providing example calculations for real practical problems.
SCOPE
The gas dispersion guide contains the following Parts:
1 Fundamentals of meteorology.
2 Overview of air quality standards.
3 Comparison between different air quality models.
4 Designing a stack.
5 Dense gas dispersion.
6 Calculation of source terms.
7 Building wake effects.
8 Overview of the chemistry of the oxides of nitrogen.
9 Overview of the ADMS complex terrain module.
10 Overview of the ADMS deposition module.
11 ADMS examples.
12 Modeling odorous releases.
13 Bibliography of useful gas dispersion books and reports.
14 Glossary of gas dispersion modeling terms.
Appendix A : Modeling Wind Generation of Particulates.
APPENDIX B TABLE OF PROPERTY VALUES FOR SPECIFIC CHEMICALS
This was my pharmaceutics presentation for mixing. Provides definitions, mechanism, types of mixers etc.
P.S: I am not the sole presenter. Ideas are from my two other colleagues as well.
Distillation Sequences, Complex Columns and Heat IntegrationGerard B. Hawkins
Distillation Sequences, Complex Columns and Heat Integration
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 SEQUENCING OF SIMPLE COLUMNS
4.1 Sidestream Columns
4.2 Multi-Feed Columns
5 SIMPLE COLUMN SEQUENCING AND HEAT
INTEGRATION INTERACTIONS
5.1 Energy Quantity and Quality
5.2 Heat Integration within the Total Flowsheet
6 COMPLEX COLUMN ARRANGEMENTS
6.1 Indirect Sequence with Vapor Link
6.2 Sidestream Systems
6.3 Pre-Fractionator Systems
7 COMPLEX COLUMNS AND HEAT INTEGRATION
INTERACTIONS
FIGURES
1 DIRECT AND INDIRECT SEQUENCES
2 A SINGLE SIDESTREAM COLUMN REPLACING 2
SIMPLE COLUMNS
3 A TYPICAL MULTI-FEED COLUMN
4 TYPICAL GRAND COMPOSITION CURVE
5 TYPICAL INDIRECT SEQUENCE WITH VAPOUR LINK
6 SIDESTREAM STRIPPER AND SIDESTREAM
RECTIFIER
7 SIMPLEST PRE-FRACTIONATOR SYSTEM
8 SIMPLEST PRE-FRACTIONATOR SYSTEM
9 PETLYUK COLUMN
Data Sources For Calculating Chemical Reaction EquilibriaGerard B. Hawkins
Data Sources For Calculating Chemical Reaction Equilibria
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 BACKGROUND TO THEORY
5 BIBLIOGRAPHY
Chemical Process Conception
0 INTRODUCTION / PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 PRODUCT STRATEGY
4.1 General
4.2 Market for the Product
4.3 Production Costs
4.4 Process Technology
5 PRELIMINARY PROCESS INFORMATION
6 REACTION AND REACTOR
6.1 Batch vs Continuous
6.2 Multiple Reactors
7 RECYCLE
7.1 Recycle Structure
7.2 Classification of Chemicals
7.3 Effect of Recycle
7.4 Preliminary Estimation of Conversion
8 REACTOR TYPE AND PERFORMANCE
8.1 Conversion-Yield Effects
8.2 Heat Effects
8.3 Equilibrium Effects
8.4 Kinetic Effects
8.5 More Help with Reactor Design
9 SEPARATION SYSTEM
10 REVIEW
11 BIBLIOGRAPHY AND REFERENCES
11.1 Preliminary Flowsheeting
11.2 Physical Properties
11.3 Reactors
11.4 Separation
11.5 Costing
APPENDICES
A BASIC REACTOR SYSTEM DESIGN
B DISCUSSION BETWEEN A CHEMIST AND A
CHEMICAL ENGINEER
C BASIC SEPARATION STRATEGY
TABLES
1 CLASSIFICATION OF MATERIALS
FIGURES
1 FLOWCHART OF THE ITERATIVE PROCEDURE REQUIRED IN PROCESS AND PRODUCT SELECTION AND DEVELOPMENT
Filtration
0 INTRODUCTION
1 The Theory Underlying Filtration Processes
1.1 The Mechanism of Simple Filtration Systems
1.1.2 Cake Filtration
1.1.3 Complete Blocking
1.1.4 Standard Blocking
1.1.5 Intermediate Blocking
1.2 Cake Filtration – Models and Mechanisms
1.2.1 Classical Theory for the Permeability of Porous Cakes and Beds
1.2.2 The Rate of Filtration through a Compressible Cake – The Standard Filtration Equation
1.2.3 The Compression or Consolidation of Filter Cakes – Ultimate degree of dewatering
1.2.4 The Rate of Consolidation
1.2.5 Useful Semi-Empirical Relations for Constant Pressure and Constant Rate Cake Filtration
1.2.6 Constant Pressure Filtration
1.2.7 Constant Rate Filtration
1.2.8 Multiphase Theory of Filtration
1.3 Crossflow Filtration
2 The Range and Selection of Filtration Equipment Technology
2.1 Scale
2.2 Solids Recovery, Liquids Clarification or Feed stream Concentration
2.3 Rate of Sedimentation
2.4 Rate of Cake Formation and Drainage
2.5 Batch vs Continuous Operation
2.6 Solids Loading
2.7 Further Processing
2.8 Aseptic or “Hygienic” Operation
2.9 Miscellaneous
2.10 Shear versus Compressional Deformation
2.11 Pressure versus Vacuum
3 Suspension Conditioning Prior to Filtration
3.1 Simple Filtration Aids
3.2 Mechanical Treatments
4 Post-Filtration Treatments and Further Downstream Processing
4.1 Washing
4.1.1 Air-Blowing
4.1.2 Drying
5 Testing and Characterization of Suspensions
5.1 Introduction – Suspension
5.2 Properties relevant to Filtration Performance
5.2.1 Pre-Filtration Properties of Suspension
5.2.2 Properties of Filter Cake
5.2.3 Laboratory Scale Filtration Rigs
5.3 Means of Monitoring Flocculant Dosage
5.4 Filter Cake Testing
5.4.1 Strength Testing (See also piston press described earlier)
5.4.2 Cake Permeability or Resistance
5.4.3 Rate of Cake Formation
6 Examples of the Application of the Forgoing Principles
6.1 Dewatering of Calcium Carbonate Slurries
6.2 Dewatering of Organic Products – Procion Dyestuffs
6.3 Filtration of Biological Systems – Harvesting a Filamentous Organism
References
Tables
Figures
Gas Mixing
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 RECOMMENDATIONS FOR GAS MIXING:
PLUG FLOW
5 RECOMMENDATIONS FOR GAS MIXING:
BACKMIXED INITIAL ZONE
6 BIBLIOGRAPHY
Physical properties and thermochemistry for reactor technologyGerard B. Hawkins
Physical Properties and Thermochemistry for Reactor Technology
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 PHYSICAL PROPERTIES
4.1 Form of Equations
4.2 The Physical Property System: “The VAULT”
4.3 Physical Property Programs
4.4 Physical Property Estimation
4.5 Sources of Expertise
5 INTERFACING COMPUTER PROGRAMS TO THE
GBHE VAULT PHYSICAL PROPERTIES PACKAGE
5.1 Preparation of the Physical Property Data
6 THERMOCHEMISTRY
6.1 Hess's Law
6.2 Standard States
6.3 Heats of Formation
6.4 Determination of Heats of Reaction
7 CALCULATION OF HEATS OF REACTION
7.1 Analogous Reactions
7.2 Heat of Formation Data Compilations
7.3 Estimation of Standard Heats of Formation
7.4 Heats of Neutralization
7.5 Temperature Effect on Heat of Reaction
8 HEATS OF SOLUTION, DILUTION AND MIXING
8.1 Calculation of Heats of Solution / Dilution from
Literature Data
8.2 Estimation of Heats of Solution and Mixing
8.3 Integral and Differential Heats
9 EXPERIMENTAL DETERMINATION OF
THERMOCHEMICAL PARAMETERS
9.1 Isoperibol Calorimetry for Heats of Reaction and Solution
9.2 Heat Flow Calorimetry
9.3 Adiabatic Calorimeter
9.4 Differential Scanning Calorimetry
10 COMPUTER CALCULATION OF ENTHALPY OR
TEMPERATURE
11 BIBLIOGRAPHY
Residence Time Distribution Data
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 BASICS OF RESIDENCE TIME DISTRIBUTION DATA
5 USE OF RESIDENCE TIME DISTRIBUTION DATA
5.1 Micromixing and Macromixing
5.2 Example 1 - Reaction is First Order
5.3 Example 2 - Reaction is Second Order
5.4 Complex Reactions and Residence Time Distribution
5.5 Examples
6 RESIDENCE TIME MEASUREMENTS WITH
RADIOISOTOPES
6.1 General
6.2 Types of Reactors
6.3 Models Based on Method of Moments
6.4 Non-impulse Input
6.5 Diagnosis of Problems
6.6 Commercial Radioisotope Service
7 BIBLIOGRAPHY
Hydrogen Compressors
Engineering Design Guide
1 SCOPE
2 PHYSICAL ROPERTIES
2.1 Data for Pure Hydrogen
2.2 Influence of Impurities
3 MATERIALS OF CONSTRUCTION
3.1 Hydrogen from Electrolytic Cells
3.2 Pure Hydrogen
4 DESIGN
4.1 Pulsation
4.2 Bypass
5 TESTING OR COMMISSIONING RECIPROCATING COMPRESSORS
6 LUBRICATION
7 LAYOUT
8 REFERENCES
FIGURES
1 MOLLIER CHART - HYDROGEN
2 COMPRESSIBILITY CHART
3 NELSON DIAGRAM
4 WATER CONTENT IN HYDROGEN FOR OIL-LUBRICATED COMPRESSORS AS GRAMM/M2 SWEPT CYLINDER AREA
OVERVIEW - FIXED BED ADSORBER DESIGN GUIDELINES
Fixed-bed adsorber design is based upon the following considerations:
• Adsorbent bed profile and media loading capacity characteristics for the specific application and adsorbent material used.
• Pressure drop characteristics across the adsorbent bed.
• Reaction kinetics.
Typically, adsorber design entails use of the following methodology:
• Adsorbent selection based upon performance and application information.
• Bed sizing based upon adsorbent loading data and service life requirements.
• Bed sizing adjustment based upon pressure drop criteria.
• Bed sizing adjustment based upon reaction kinetics criteria.
A discussion of each design consideration follows.
VLE Data - Selection and Use
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 DIAGRAMMATIC REPRESENTATION OF IDEAL
AND NON-IDEAL SYSTEMS
4.1 Ideal Mixtures
4.2 Non-Ideal Mixtures
5 REVIEW OF VLE MODELS
5.1 Ideal Behavior in Both Phases
5.2 Liquid Phase Non-Idealities
5.3 High Pressure Systems
5.4 Special Models
6 SETTING UP A VLE MODEL
6.1 Define Problem
6.2 Select Data
6.3 Select Correlation(s)
6.4 Produce Model
7 AVOIDING PITFALLS
7.1 Experimental Data is Better than Estimates
7.2 Check Validity of Fitted Model
7.3 Check Limitations of Estimation Methods
7.4 Know Your System
7.5 Appreciate Errors and Effects
7.6 If in Doubt – Ask
8 A CASE STUDY
8.1 The Problem
8.2 The System
8.3 Data Available
8.4 Selected Correlation
8.5 Simulation
8.6 Selection of Model
9 RECOMMENDED READING
10 VLE EXPERTS IN GBHE
APPENDICES
A USE OF EXTENDED ANTOINE EQUATION
B USE OF WILSON EQUATION
C USEFUL METHODS OF ESTIMATING
D EQUATIONS OF STATE FOR VLE CALCULATIONS
TABLES
1 SUMMARY OF VLE METHODS
2 LIST OF USEFUL REFERENCES
FIGURES
1 VAPOR-LIQUID EQUILIBRIUM - IDEAL SOLUTION
BEHAVIOR
2 VAPOR-LIQUID EQUILIBRIUM - A GENERALISED
Y-X DIAGRAM
3 VAPOR-LIQUID EQUILIBRIUM - MINIMUM BOILING
AZEOTROPE
4 VAPOR-LIQUID EQUILIBRIUM - MAXIMUM BOILING
AZEOTROPE
5 VAPOR-LIQUID EQUILIBRIUM - MINIMUM BOILING
AZEOTROPE -TWO LIQUID PHASES
6 SENSITIVITY TO ERROR IN VLE DATA (BASED ON FENSKE EQUATION)
7(a) FITTING WILSON 'A' VALUES TO VLE DATA - CASE A
7(b) FITTING WILSON 'A' VALUES TO VLE DATA - CASE B
7(c) FITTING WILSON 'A' VALUES TO VLE DATA - CASE C
Solid Catalyzed Gas Phase Reactor Selection
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 ADIABATIC REACTORS
4.1 Single Bed Reactors
4.2 Divided Bed Reactors
4.3 Moving Bed Reactors
4.4 Radial Flow Reactors
5 NON ADIABATIC REACTORS
5.1 Tubular Reactor with External Heating/Cooling
5.2 Tube Cooled Reactors
5.3 Autothermal Reactors
5.4 Hot/Cold Shot Reactors
5.5 Divided Bed Reactors with Intercooling
5.6 Radial Flow Reactors with Intercooling
5.7 Fluid Bed Reactors
6 NOTES ON USING REACTOR SELECTION
GUIDE (TABLE 1)
TABLE
1 REACTOR SELECTION GUIDE
FIGURES
1 TUBULAR REACTOR: EXAMPLE OF CATALYST IN ANNULAR TUBES COOLED BY STEAM RAISING
2 AUTOTHERMAL REACTOR: CATALYST BED COOLED BY INFLOWING GAS IN TUBES
3 COLD SHOT CONVERTER: FIXED ADIABATIC BEDS WITH INTERBED QUENCH GAS MIXING
Turbulent Heat Transfer to Non Newtonian Fluids in Circular TubesGerard B. Hawkins
Turbulent Heat Transfer to Non Newtonian Fluids in Circular Tubes
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 THE INTEGRATION OF THE ENERGY EQUATION
5 THE EDDY VISCOSITY FOR NON-NEWTONIAN AND DRAG REDUCING FLUIDS
6 THE CALCULATION OF HEAT TRANSFER
COEFFICIENTS FOR NON-NEWTONIAN AND DRAG
REDUCING FLUIDS IN TURBULENT PIPE FLOW
6.1 General
6.2 Drag Reducing Fibre Suspensions
6.3 Transition Delay
7 NOMENCLATURE
8 BIBLIOGRAPHY
SYNOPSIS
The principles underlying centrifugal separation of particulate species are briefly considered, and the main types of separator available are noted. The procedures available for scale-up from laboratory or semi-technical data are then discussed in detail with particular reference to perhaps the most important class of machine for fine particle processing: the disc-nozzle centrifuge.
Starting with the basic concepts behind their design, discussion follows to explain the factors which may limit centrifuge performance. It is shown how a few simple; laboratory scale tests can give a valuable insight into the design and operation of full-scale industrial machines.
Large Water Pumps
CONTENTS
1 SCOPE
SECTION ONE: INTEGRATION OF PUMPS INTO THE PROCESS
2 PROPERTIES OF FLUID
2.1 Cooling Water
2.2 Brine
2.3 Estuary Water
2.4 Harbor Water
2.5 Oil-field water
3 CALCULATION OF DUTY
4 CHOICE OF TYPE AND NUMBER OF PUMPS
4.1 Type of Pump
4.2 Points to Consider
4.3 Number of Pumps
5 RECOMMENDED LINE DIAGRAM
5.1 Check List for Each Pump
6 RECOMMENDED LAYOUT
SECTION TWO: CONSTRUCTION FEATURES
7 HORIZONTAL, AXIALLY SPLIT CASING PUMPS
7.1 Pressure Casing
7.2 Bolting
7.3 Flanges and Connections
7.4 Rotating Elements
7.5 Wear Rings
7.6 Running Clearances
7.7 Mechanical Seals
7.8 Packed Glands
7.9 Bearings and Bearing Housings
7.10 Lubrication
7.11 Couplings
7.12 Guards
7.13 Baseplates
7.14 Flywheels
8 VERTICAL PUMPS
8.1 General
8.2 Pressure Casing
8.3 Bolting
8.4 Flanges and Connections
8.5 Rotating Element
8.6 Packed Glands
8.7 Bearings and Bearing Housings
8.8 Pump Head
8.9 Column Pipes
8.10 Line Shaft and Couplings
8.11 Reverse Rotation
8.12 Gearboxes
9 MATERIALS
9.1 Castings
9.2 Casings
9.3 Impellers
9.4 Shafts
9.5 Shaft Sleeves
9.6 Bolts and Nuts
10 DRIVERS
10.1 Electric Motor Drives
11 BIBLIOGRAPHY
APPENDICES:
A COOLING WATER - EUROPEAN SITE
B TIDAL RIVER ESTUARY
C FLYWHEEL INERTIA FOR PRESSURE SURGE ABATEMENT
D RESIN COATING OF CASINGS FOR WATER PUMPS
E AREA RATIO METHOD
F NOTES ON PUMP IMPELLERS CASTINGS
G LIMIT ON SHAFT DIAMETER FOR HORIZONTAL PUMPS HAVING
ONE DOUBLE-ENTRY IMPELLER SUPPORTED BETWEEN BEARINGS
H FORCES AND BENDING MOMENTS ON RISING MAIN ASSEMBLY
I POWER COSTS
J PUTATIVE COST COMPARISON SHEET
K TECHNICAL COMPARISON SHEETS
FIGURES
2.1 VAPOR TEMPERATURE CURVES
2.2 DENSITY TEMPERATURE CURVES
3.1 TYPICAL HEAD OF PUMPS
3.2 TOTAL HEAD OF VERTICAL IMMERSED PUMP
3.3 TYPICAL TIDAL RIVER ESTUARY LEVELS
3.5 SUBMERGENCE LIMITS
4.1 TYPES OF PUMP
4.2 GUIDE TO PUMP TYPE AND SPEED
5.1 TYPICAL LINE DIAGRAM
6 GUIDE TO SUCTION PIPEWORK DESIGN
7 CASING AND IMPELLER DETAILS
8.1 DRY WELL AND WET WELL PUMP INSTALLATIONS
8.2 BELLMOUTH DIMENSIONS FOR VERTICAL INTAKES
8.3 MAXIMUM SPACING BETWEEN SHAFT GUIDE BUSHING
8.4 LINE SHAFT COUPLING
9 TYPICAL VOLUTE CASING
10 TYPICAL CASE WEAR RINGS
11 SEAL AREA
TABLES
1 LIQUID PROPERTIES SODIUM CHLORIDE (25% W/W)
2 LIQUID PROPERTIES SODIUM CHLORIDE (20% W/W)
3 LIQUID PROPERTIES SODIUM CHLORIDE (16.25% W/W)
4 LIQUID PROPERTIES SODIUM CHLORIDE (15% W/W)
5 LIQUID PROPERTIES SODIUM CHLORIDE (10% W/W)
6 LIQUID PROPERTIES SODIUM CHLORIDE (5% W/W)
7 GUIDE TO PUMP TYPE AND SPEED
8 RECOMMENDED CAST MATERIALS FOR USE IN THE PUMP INDUSTRY
GRAPHS
1 GUIDE TO ROTOR INERTIA
2 LIMITS BETWEEN BEARINGS
DOCUMENTS REFERRED TO IN THIS ENGINEERING DEPARTMENT DESIGN GUIDE
Fluid Separation
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 A SEPARATION LOGIC TREE
5 METHODS OF DISTILLATION
5.1 Fractional Distillation
5.2 Azeotropic Distillation
5.3 Extractive Distillation
6 LIQUID-LIQUID EXTRACTION
7 OTHER COMMERCIAL METHODS OF SEPARATION
7.1 Adsorption
7.2 Fractional Crystallization
7.3 Ion Exchange
7.4 Membrane Processes
7.4.1 Ultrafiltration
7.4.2 Reverse Osmosis
7.4.3 Pervaporation
7.4.4 Liquid Membranes
7.4.5 Gas Permeation
7.4.6 Dialysis
7.4.7 Electrodialysis
7.5 Supercritical Fluid Extraction
7.6 Dissociation Extraction
7.7 Foam Fractionation
7.8 Clathration
7.9 Chromatography
8. OTHER METHODS OF SEPARATION
8.1 Precipitation
8.2 Paper Chromatography
8.3 Ligand Specific Chromatography
8.4 Electrophoresis
8.5 Isoelectric Focusing
8.6 Thermal Diffusion
8.7 Sedimentation Ultracentrifugation
8.8 Isopycnic Ultracentrifugation
8.9 Molecular Distillation
8.10 Gel Filtration
APPENDICES
A AT A GLANCE CHART BASED ON FENSKE, UNDERWOOD
B A GENERALIZED y - x DIAGRAM
C TEMPERATURE - COMPOSITION DIAGRAMS FOR
AZEOTROPIC MIXTURES
D A TYPICAL y - x DIAGRAM FOR EXTRACTIVE DISTILLATION (SOLVENT FREE BASIS)
E RAPID ESTIMATION OF LIQUID-LIQUID EXTRACTION REQUIREMENTS
F LIQUID - LIQUID EXTRACTION - THE USE OF EXTRACT REFLUX
G SELECTIVITIES REQUIRED FOR EQUAL PLANT COSTS
FIGURE
1 SEPARATION LOGIC TREE
Pipeline Design for Isothermal, Laminar Flow of Non-Newtonian FluidsGerard B. Hawkins
Pipeline Design for Isothermal, Laminar Flow of Non-Newtonian Fluids
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 RHEOLOGICAL BEHAVIOR OF PURELY VISCOUS
NON-NEWTONIAN FLUIDS
4.1 Experimental Characterization
4.2 Rheological Models
5 PRESSURE DROP-FLOW RATE RELATIONSHIPS
BASED DIRECTLY ON EXPERIMENTAL DATA
5.1 Use of Shear Stress – Shear Rate Data
5.2 Tubular Viscometer Data
6 PRESSURE DROP – FLOW RATE RELATIONSHIPS BASED ON RHEOLOGICAL MODELS
7 LOSSES IN PIPE FITTINGS
7.1 Entrances Losses
7.2 Expansion Effects
7.3 Contraction Losses
7.4 Valves
7.5 Bends
8 EFFECT OF WALL SLIP
9 VELOCITY PROFILES
9.1 Velocity Profile from Experimental Flow-Curve
9.2 Velocity Profile from Rheological Model
9.3 Residence Time Distribution
10 CHECKS ON THE VALIDITY OF THE
DESIGN PROCEDURES
10.1 Rheological Behavior
10.2 Validity of Experimental Data
10.2 Check on Laminar Flow
11 NOMENCLATURE
12 REFERENCES
FIGURES
1 FLOW CURVES FOR PURELY VISCOUS FLUIDS
2 PLOTS OF D∆P/4L VERSUS 32Q/ɳD3 FOR PURELY VISCOUS FLUIDS
3 LOG-LOG PLOT OF t VERSUS ý
4 FLOW CURVE FOR A BINGHAM PLASTIC
5 LOG-LOG PLOT FOR A GENERALIZED BINGHAM
PLASTIC
6 CORRELATION OF ENTRANCE LOSS
7 CORRELATION OF EXPANSION LOSS
8 EFFECT OF “WALL SLIP” ON VELOCITY PROFILE
9 D∆P/4L VERSUS Q/ɳR3 WITH WALL SLIP
10 EVALUATION OFUs WITH Ʈw
11 VARIATION OF Us WITH Ʈw
12 PLOT OF D∆P/4L VERSUS 8 (ū- Us)/D FOR
CONDITIONS OF WALL SLIP
13 CUMULATIVE RESIDENCE TIME DISTRIBUTION
TO POWER LAW FLUIDS
14 EFFECTS OF TUBE LENGTH AND DIAMETER ON
RELATIONSHIP BETWEEN D∆P/4L AND 32Q/ɳD3
Fouling Resistances for Cooling Water
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 GENERAL
5 COOLING WATER FOULING
6 CHROMATE SYSTEMS
6.1 General
6.2 Constraints
6.3 Requirements
6.4 Fouling resistances
7 NON-CHROMATE SYSTEMS
7.1 General
7.2 Requirements and Constraints
7.3 Fouling resistances
8 UNTREATED COOLING WATER
9 MATERIALS OTHER THAN MILD STEEL
APPENDICES
A FOULING RESISTANCES FOR COOLING WATER
B FOULING FILM THICKNESS
Pressure Relief Systems Vol 2
Causes of Relief Situations
This Volume 2 is a guide to the qualitative identification of common causes of overpressure in process equipment. It cannot be exhaustive; the process engineer and relief systems team should look for any credible situation in addition to those given in this Part which could lead to a need for pressure relief (a relief situation).
Pressure Relief Systems
BACKGROUND TO RELIEF SYSTEM DESIGN Vol.1 of 6
The Guide has been written to advise those involved in the design and engineering of pressure relief systems. It takes the user from the initial identification of potential causes of overpressure or under pressure through the process design of relief systems to the detailed mechanical design. "Hazard Studies" and quantitative hazards analysis are not described; these are seen as complementary activities. Typical users of the Guide will use some Parts in detail and others in overview.
Theory of Carbon Formation in Steam Reforming
Contents
1 Introduction
2 Underpinning Theory
2.1 Conceptualization
2.2 Reforming Reactions
2.3 Carbon Formation Chemistry
2.3.1 Natural Gas
2.3.2 Carbon Formation for Naphtha Feeds
2.3.3 Carbon Gasification
2.4 Heat Transfer
3 Causes
3.1 Effects of Carbon Formation
3.2 Types of Carbon
4 What are the Effects of Carbon Formation?
4.1 Why does Carbon Formation Get Worse?
4.1.1 So what is the Next Step?
4.2 Consequences of Carbon Formation
4.3 Why does Carbon Form where it does?
4.3.1 Effect on Process Gas Temperature
4.4 Why does Carbon Formation Propagate Down the Tube?
4.4.1 Effect on Radiation on the Fluegas Side
4.5 Why does Carbon Formation propagate Up the Tube?
5 How do we Prevent Carbon Formation
5.1 The Role of Potash
5.2 Inclusion of Pre-reformer
5.3 Primary Reformer Catalyst Parameters
5.3.1 Activity
5.3.2 Heat Transfer
5.3.3 Increased Steam to Carbon Ratio
6 Steam Out
6.1 Why does increasing the Steam to Carbon Ratio Not Work?
6.2 Why does reducing the Feed Rate not help?
6.3 Fundamental Principles of Steam Outs
TABLES
1 Heat Transfer Coefficients in a Typical Reformer
2 Typical Catalyst Loading Options
FIGURES
1 Hot Bands
2 Conceptual Pellet
3 Naphtha Carbon Formation
4 Heat Transfer within an Reformer
5 Types of Carbon Formation
6 Effect of Carbon on Nickel Crystallites
7 Absorption of Heat
8 Comparison of "Base Case" v Carbon Forming Tube
9 Carbon Formation Vicious Circle
10 Temperature Profiles
11 Carbon Pinch Point
12 Carbon Formation
13 Effect on Process Gas Temperature
14 How does Carbon Propagate into an Unaffected Zone?
15 Movement of the Carbon Forming Region
16 Effect of Hot Bands on Radiative Heat Transfer
17 Effect of Potash on Carbon Formation
18 Application of a Pre-reformer
19 Effect of Activity on Carbon Formation
Calculation of an Ammonia Plant Energy Consumption: Gerard B. Hawkins
Calculation of an Ammonia Plant Energy Consumption:
Case Study: #06023300
Plant Note Book Series: PNBS-0602
CONTENTS
0 SCOPE
1 CALCULATION OF NATURAL GAS PROCESS FEED CONSUMPTION
2 CALCULATION OF NATURAL GAS PROCESS FUEL CONSUMPTION
3 CALCULATION OF NATURAL GAS CONSUMPTION FOR PILOT BURNERS OF FLARES
4 CALCULATION OF DEMIN. WATER FROM DEMIN. UNIT
5 CALCULATION OF DEMIN. WATER TO PACKAGE BOILERS
6 CALCULATION OF MP STEAM EXPORT
7 CALCULATION OF LP STEAM IMPORT
8 DETERMINATION OF ELECTRIC POWER CONSUMPTION
9 DETERMINATION OF THE TOTAL ENERGY CONSUMPTION OF THE AMMONIA PLANT ISBL
10 ADJUSTMENT OF ELECTRIC POWER CONSUMPTION FOR TEST RUN CONDITIONS
11 CALCULATION OF AMMONIA SHARE IN MP STEAM CONSUMPTION IN UTILITIES
12 CALCULATION OF AMMONIA SHARE IN ELECTRIC POWER CONSUMPTION IN UTILITIES
13 DETERMINATION OF THE TOTAL ENERGY CONSUMPTION OF THE AMMONIA PLANT OSBL
14 DETERMINATION OF THE TOTAL ENERGY CONSUMPTION OF THE AMMONIA PLANT
Ammonia Plant Technology
Pre-Commissioning Best Practices
GBHE-APT-0102
PICKLING & PASSIVATION
CONTENTS
1 PURPOSE OF THE WORK
2 CHEMICAL CONCEPT
3 TECHNICAL CONCEPT
4 WASTES & SAFETY CONCEPT
5 TARGET RESULTS
6 THE GENERAL CLEANING SEQUENCE MANAGEMENT
6.6.1 Pre-cleaning or “Physical Cleaning
6.6.2 Pre-rinsing
6.6.3 Chemical Cleaning
6.6.4 Critical Factors in Cleaning Success
6.6.5 Rinsing
6.6.6 Inspection and Re-Cleaning, if Necessary
7 Systems to be treated by Pickling/Passivation
Ammonia Plant Technology
Pre-Commissioning Best Practices
Piping and Vessels Flushing and Cleaning Procedure
CONTENTS
1 Scope
2 Aim/purpose
3 Responsibilities
4 Procedure
4.1 Main cleaning methods
4.1.1 Mechanical cleaning
4.1.2 Cleaning with air
4.1.3 Cleaning with steam (for steam networks only)
4.1.4 Cleaning with water
4.2 Choice of the cleaning method
4.3 Cleaning preparation
4.4 Protection of the devices included in the network
4.5 Protection of devices in the vicinity of the network
4.6 Water flushing procedure
4.6.1 Specific problems of water flushing
4.6.2 Preparation for water flushing
4.6.3 Performing a water flush
4.6.4 Cleanliness criteria
4.7 Air blowing procedure
4.7.1 Specific problems of air blowing
4.7.2 Preparation for air blowing
4.7.3 Performing air blowing
4.7.4 Cleanliness checks
4.8 Steam blowing procedure
4.8.1 Specific problems of steam blowing
4.8.2 Preparation for steam blowing
4.8.3 Performing steam blowing
4.8.4 Cleanliness checks
4.9 Chemical cleaning procedure
4.9.1 Specific problems of cleaning with a chemical solution
4.9.2 Preparation for chemical cleaning
4.9.3 Performing a chemical cleaning
4.9.4 Cleanliness criteria
4.10 Re-assembly - general guideline
4.11 Preservation of flushed piping
DESIGN OF VENT GAS COLLECTION AND DESTRUCTION SYSTEMS Gerard B. Hawkins
DESIGN OF VENT GAS COLLECTION AND DESTRUCTION SYSTEMS
CONTENTS
1 INTRODUCTION
1.1 Purpose
1.2 Scope of this Guide
1.3 Use of the Guide
2 ENVIRONMENTAL ISSUES
2.1 Principal Concerns
2.2 Mechanisms for Ozone Formation
2.3 Photochemical Ozone Creation Potential
2.4 Health and Environmental Effects
2.5 Air Quality Standards for Ground Level Concentrations of Ozone, Targets for Reduction of VOC Discharges and Statutory Discharge Limits
3 VENTS REDUCTION PHILOSOPHY
3.1 Reduction at Source
3.2 End-of-pipe Treatment
4 METHODOLOGY FOR COLLECTION & ASSESSMENT OF PROCESS FLOW DATA
4.1 General
4.2 Identification of Vent Sources
4.3 Characterization of Vents
4.4 Quantification of Process Vent Flows
4.5 Component Flammability Data Collection
4.6 Identification of Operating Scenarios
4.7 Quantification of Flammability Characteristics for Combined Vents
4.8 Identification, Quantification and Assessment of Possibility of Air Ingress Routes
4.9 Tabulation of Data
4.10 Hazard Study and Risk Assessment
4.11 Note on Aqueous / Organic Wastes
4.12 Complexity of Systems
4.13 Summary
5 SAFE DESIGN OF VENT COLLECTION HEADER SYSTEMS
5.1 General
5.2 Process Design of Vent Headers
5.3 Liquid in Vent Headers
5.4 Materials of Construction
5.5 Static Electricity Hazard
5.6 Diversion Systems
5.7 Snuffing Systems
6 SAFE DESIGN OF THERMAL OXIDISERS
6.1 Introduction
6.2 Design Basis
6.3 Types of High Temperature Thermal Oxidizer
6.4 Refractories
6.5 Flue Gas Treatment
6.6 Control and Safety Systems
6.7 Project Program
6.8 Commissioning
6.9 Operational and Maintenance Management
APPENDICES
A GLOSSARY
B FLAMMABILITY
C EXAMPLE PROFORMA
D REFERENCES
DOCUMENTS REFERRED TO IN THIS PROCESS GUIDE
TABLE
1 PHOTOCHEMICAL OZONE CREATION POTENTIAL REFERENCED
TO ETHYLENE AS UNITY
FIGURES
1 SCHEMATIC OF TYPICAL VENT COLLECTION AND THERMAL OXIDIZER SYSTEM
2 TYPICAL KNOCK-OUT POT WITH LUTED DRAIN
3 SCHEMATIC OF DIVERSION SYSTEM
4 CONVENTIONAL VERTICAL THERMAL OXIDIZER
5 CONVENTIONAL OXIDIZER WITH INTEGRAL WATER SPARGER
6 THERMAL OXIDIZER WITH STAGED AIR INJECTION
7 DOWN-FIRED UNIT WITH WATER BATH QUENCH
8 FLAMELESS THERMAL OXIDATION UNIT
9 THERMAL OXIDIZER WITH REGENERATIVE HEAT RECOVERY
10 TYPICAL PROJECT PROGRAM
11 TYPICAL FLAMMABILITY DIAGRAM
12 EFFECT OF DILUTION WITH AIR
13 EFFECT OF DILUTION WITH AIR ON 100 Rm³ OF FLAMMABLE GAS
PRACTICAL GUIDE ON THE SELECTION OF PROCESS TECHNOLOGY FOR THE TREATMENT OF A...Gerard B. Hawkins
PRACTICAL GUIDE ON THE SELECTION OF PROCESS TECHNOLOGY FOR THE TREATMENT OF AQUEOUS ORGANIC EFFLUENT STREAMS
CONTENTS
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
3.1 IPU
3.2 AOS
3.3 BODs
3.4 COD
3.5 TOC
3.6 Toxicity
3.7 Refractory Organics/Hard COD
3.8 Heavy Metals
3.9 EA
3.10 Biological Treatment Terms
3.11 BATNEEC
3.12 BPEO
3.13 EQS/LV
3.14 IPC
3.15 VOC
3.16 F/M Ratio
3.17 MLSS
3.18 MLVSS
4 DESIGN/ECONOMIC GUIDELINES
5 EUROPEAN LEGISLATION
5.1 General
5.2 Integrated Pollution Control (IPC)
5.3 Best Available Techniques Not Entailing Excessive Costs (BATNEEC)
5.4 Best Practicable Environmental Option (BPEO)
5.5 Environmental Quality Standards(EQS)
6 IPU EXIT CONCENTRATION
7 SITE/LOCAL REQUIREMENTS
8 PROCESS SELECTION PROCEDURE
8.1 Waste Minimization Techniques (WMT)
8.2 AOS Stream Definition
8.3 Technical Check List
8.4 Preliminary Selection of Suitable Technologies
8.5 Process Sequences
8.6 Economic Evaluation
8.7 Process Selection
APPENDICES
A DIRECTIVE 76/464/EEC - LIST 1
B DIRECTIVE 76/464/EEC - LIST 2
C THE EUROPEAN COMMISSION PRIORITY CANDIDATE LIST
D THE UK RED LIST
E CURRENT VALUES FOR EUROPEAN COMMUNITY ENVIRONMENTAL QUALITY STANDARDS AND CORRESPONDING LIMIT VALUES
F ESTABLISHED TECHNOLOGIES
G EMERGING TECHNOLOGY
H PROPRIETARY/LESS COMMON TECHNOLOGIES
J COMPARATIVE COST DATA
PRACTICAL GUIDE ON THE REDUCTION OF DISCHARGES TO ATMOSPHERE OF VOLATILE ORGA...Gerard B. Hawkins
PRACTICAL GUIDE ON THE REDUCTION OF DISCHARGES TO ATMOSPHERE OF VOLATILE ORGANIC COMPOUNDS (VOCs)
FOREWORD
CONTENTS
1 INTRODUCTION
2 THE NEED FOR VOC CONTROL
3 CONTROL AT SOURCE
3.1 Choice or Solvent
3.2 Venting Arrangements
3.3 Nitrogen Blanketing
3.4 Pump Versus Pneumatic Transfer
3.5 Batch Charging
3.6 Reduction of Volumetric Flow
3.7 Stock Tank Design
4 DISCHARGE MEASUREMENT
4.1 By Inference or Calculation
4.2 Flow Monitoring Equipment
4.3 Analytical Instruments
4.4 Vent Emissions Database
5 ABATEMENT TECHNOLOGY
5.1 Available Options
5.2 Selection of Preferred Option
5.3 Condensation
5.4 Adsorption
5.5 Absorption
5.6 Thermal Incineration
5.7 Catalytic Oxidation
5.8 Biological Filtration
5.9 Combinations of Process technologies
5.10 Processes Under Development
6 GLOSSARY OF TERMS
7 REFERENCES
Appendix 1. Photochemical Ozone Creation Potentials
Appendix 2. Examples of Adsorption Preliminary Calculations
Appendix 3. Example of Thermal Incineration Heat and Mass Balance
Appendix 4. Cost Correlations
Getting the Most Out of Your Refinery Hydrogen PlantGerard B. Hawkins
Getting the Most Out of Your Refinery Hydrogen Plant
Contents
Summary
1 Introduction
2 "On-purpose" Hydrogen Production
3 Operational Aspects
4 Uprating Options on the Steam Reformer
4.1 Steam Reforming Catalysts and Tube Metallurgy
4.2 Oxygen-blown Secondary Reformer
4.3 Pre-reforming
4.4 Post-reforming
5 Downstream Units
6 Summary of Uprating Options
7 Conclusions
EMERGENCY ISOLATION OF CHEMICAL PLANTS
CONTENTS
1 Introduction
2 When should Emergency Isolation Valves be Installed
3 Emergency Isolation Valves and Associated Equipment
3.1 Installations on existing plant
3.2 Actuators
3.3 Power to close or power to open
3.4 The need for testing
3.5 Hand operated Emergency Valves
3.6 The need to stop pumps in an emergency
3.7 Location of Operating Buttons
3.8 Use of control valves for Isolation
4 Detection of Leaks and Fires
5 Precautions during Maintenance
6 Training Operators to use Emergency Isolation Valves
7 Emergency Isolation when no remotely operated valve is available
References
Glossary
Appendix I Some Fires or Serious Escapes of Flammable Gases or Liquids that could have been controlled by Emergency Isolation Valves
Appendix II Some typical Installations
Amine Gas Treating Unit - Best Practices - Troubleshooting Guide Gerard B. Hawkins
Amine Gas Treating Unit Best Practices - Troubleshooting Guide for H2S/CO2 Amine Systems
Contents
Process Capabilities for gas treating process
Typical Amine Treating
Typical Amine System Improvements
Primary Equipment Overview
Inlet Gas Knockout
Absorber
Three Phase Flash Tank
Lean/Rich Heat Exchanger
Regenerator
Filtration
Amine Reclaimer
Operating Difficulties Overview
Foaming
Failure to Meet Gas Specification
Solvent Losses
Corrosion
Typical Amine System Improvements
Degradation of Amines and Alkanolamines during Sour Gas Treating
APPENDIX
Best Practices - Troubleshooting Guide
LF Energy Webinar: Electrical Grid Modelling and Simulation Through PowSyBl -...DanBrown980551
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Kubernetes & AI - Beauty and the Beast !?! @KCD Istanbul 2024Tobias Schneck
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Cheryl Hung, ochery.com
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Presented by BookNet Canada on May 28, 2024, with support from the Department of Canadian Heritage.
Connector Corner: Automate dynamic content and events by pushing a buttonDianaGray10
Here is something new! In our next Connector Corner webinar, we will demonstrate how you can use a single workflow to:
Create a campaign using Mailchimp with merge tags/fields
Send an interactive Slack channel message (using buttons)
Have the message received by managers and peers along with a test email for review
But there’s more:
In a second workflow supporting the same use case, you’ll see:
Your campaign sent to target colleagues for approval
If the “Approve” button is clicked, a Jira/Zendesk ticket is created for the marketing design team
But—if the “Reject” button is pushed, colleagues will be alerted via Slack message
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And...
Speakers:
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However, this ease of use means that the subject of security in Kubernetes is often left for later, or even neglected. This exposes companies to significant risks.
In this talk, I'll show you step-by-step how to secure your Kubernetes cluster for greater peace of mind and reliability.
Essentials of Automations: Optimizing FME Workflows with ParametersSafe Software
Are you looking to streamline your workflows and boost your projects’ efficiency? Do you find yourself searching for ways to add flexibility and control over your FME workflows? If so, you’re in the right place.
Join us for an insightful dive into the world of FME parameters, a critical element in optimizing workflow efficiency. This webinar marks the beginning of our three-part “Essentials of Automation” series. This first webinar is designed to equip you with the knowledge and skills to utilize parameters effectively: enhancing the flexibility, maintainability, and user control of your FME projects.
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- Essentials of FME Parameters: Understand the pivotal role of parameters, including Reader/Writer, Transformer, User, and FME Flow categories. Discover how they are the key to unlocking automation and optimization within your workflows.
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Smart TV Buyer Insights Survey 2024 by 91mobiles.pdf91mobiles
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Mixing of Immiscible Liquids
1. GBH Enterprises, Ltd.
Process Engineering Guide:
GBHE-PEG-MIX-704
Mixing of Immiscible Liquids
Information contained in this publication or as otherwise supplied to Users is
believed to be accurate and correct at time of going to press, and is given in
good faith, but it is for the User to satisfy itself of the suitability of the information
for its own particular purpose. GBHE gives no warranty as to the fitness of this
information for any particular purpose and any implied warranty or condition
(statutory or otherwise) is excluded except to the extent that exclusion is
prevented by law. GBHE accepts no liability resulting from reliance on this
information. Freedom under Patent, Copyright and Designs cannot be assumed.
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Specializing in the Development & Commercialization of New Technology in the Refining & Petrochemical Industries
Web Site: www.GBHEnterprises.com
2. Process Engineering Guide:
Mixing of Immiscible Liquids
CONTENTS
SECTION
0
INTRODUCTION/PURPOSE
2
1
SCOPE
2
2
FIELD OF APPLICATION
2
3
DEFINITIONS
2
4
EQUIPMENT
2
4.1
4.2
4.3
Agitated Tanks
Flow Mixers
'High Shear' Mixers
2
2
2
5
SYSTEM PHYSICAL PROPERTIES
3
5.1
5.2
5.3
Density
Viscosity
Interfacial Tension
3
4
4
6
STIRRED VESSELS
4
6.1
6.2
6.3
6.4
6.5
Design for Complete Dispersion
Prediction of Phase Inversion
Design for Mass Transfer
Design for Dispersed Phase Mixing
Hold-Up in Continuous Vessels
4
5
5
6
6
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Process Technology – Ammonia Catalyst Process Technology - Methanol Catalysts / process Technology – Petrochemicals
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3. 7
FLOW MIXERS
6
7.1
7.2
Design for Turbulent Conditions
Design for Laminar Conditions
7
12
TABLES
1
REYNOLDS NUMBER RANGES
7
FIGURES
1
STANDARD TANK CONFIGURATION
3
2
EXPERIMENTAL RELATIONSHIP BETWEEN MASS
TRANSFER COEFFICIENT AND POWER DENSITY
10
DOCUMENTS REFERRED TO IN THIS PROCESS
ENGINEERING GUIDE
14
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4. 0
INTRODUCTION/PURPOSE
This Guide is one in a series of Mixing Guides and has been prepared for GBH
Enterprises.
1
SCOPE
This Guide deals with the mixing of immiscible liquids in agitated vessels and
flow (or motionless, static) mixers. It does not cover other mixing devices such as
multi-stage extractors or 'high shear' mixers.
2
FIELD OF APPLICATION
This Guide applies to Process Engineers in GBH Enterprises worldwide.
3
DEFINITIONS
No specific definitions apply to this Guide.
With the exception of terms used as proper nouns or titles, those terms with initial
capital letters which appear in this document and are not defined above are
defined in the Glossary of Engineering Terms.
4
EQUIPMENT
4.1
Agitated Tanks
Agitated stirred tanks may be used as reactors, washing or holding tanks, etc.
Mass transfer rates are generally such that phase equilibria in liquid-liquid
systems are reached within a short residence time (ca. 1 min). Standard solvent
extraction duties are not covered by this Guide.
The bulk fluid dynamics, power requirements and flow patterns in vessels
containing well-mixed two-phase liquids are generally similar to those of single
phase liquids when stirred at similar impeller Reynolds numbers.
The recommended equipment geometry for a reactor is shown in Figure 1. The
duty favors smaller D/T ratios, with a value of 0.33 recommended for general
purpose work.
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5. 4.2
Flow Mixers
Pipe flow mixers (also known as motionless or static mixers), as made by Kenics,
Sulzer and others, can be used to disperse one liquid as droplets in another. The
pressure drop supplies the energy for drop formation.
4.3
'High Shear' Mixers
'High Shear' mixers may be used for liquid-liquid mixing duties, especially when
one of the feed liquids or the resulting emulsion exhibits a high viscosity. As
these mixers are equally suitable for solid-liquid mixing, their application is the
subject of a separate Guide, GBHE-PEG-MIX-709 – High Shear Mixers.
FIGURE 1
STANDARD TANK CONFIGURATION
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6. 5
SYSTEM PHYSICAL PROPERTIES
For well-mixed systems, the following equations to represent the mixed fluid
properties are recommended, where the suffix c refers to the continuous phase
and the suffix d to the dispersed phase.
5.1
Density
The mixed system density is given by:
The Vermeulen equation:
is recommended for liquid-liquid systems.
5.3
Interfacial Tension
The interfacial tension may be required in the approximate calculation of the
droplet size, which in turn is used to estimate the interfacial area and the
volumetric mass transfer coefficient, kLa.
For liquids of low mutual solubility which are free of surfactant additives, the
difference between the pure liquid surface tensions will be a sufficiently accurate
estimate of the interfacial tension. This procedure could, however, lead to a
serious overestimate of the interfacial tension when the liquids exhibit
appreciable mutual solubility or when surfactants or dispersants are present.
In these cases the measurement of the interfacial tension is not recommended,
scale-up from small mixer trials being the preferred method.
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Web Site: www.GBHEnterprises.com
7. 6
STIRRED VESSELS
6.1
Design for Complete Dispersion
The power requirement for complete dispersion is the minimum for all duties.
This has been found to be insensitive to the interfacial properties and depends
on which phase is dispersed.
The equations for the two cases use SI units throughout. They have been
derived from experimental data on a 20 liter scale using 21 liquid pairs and are
recommended for turbine and paddle type impellers. The data obtained with
Pfaudler mixers, D/T of 0.6 and 'beaver-tail' baffles checks with published work
by Van Heuven working with standard baffles and a D/T ratio of 0.3. Scale-up on
the basis of P/V, power per unit volume, will be conservative.
6.1.1 Power Requirement for Light Phase Dispersed
Light phase fraction 0.1 to 0.9:
6.1.2 Power Requirement for Heavy Phase Dispersed
Heavy phase fraction 0.1 to 0.4:
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8. 6.1.3 Range of Variables
The ranges of variables used in the experimental work were:
Density 660 to 1620 kg/m3
Phase Density Difference 37 to 682 kg/m3
Continuous Phase Viscosity 0.00031 to 0.0173 N.s/m2
Dispersed Phase Viscosity 0.00031 to 0.0173 N.s/m2
Interfacial Tension 0.019 to 0.064 N/m
6.2
Prediction of Phase Inversion
6.2.1 Hydrophilic/Lipophilic Balance (HLB)
Dispersed phase volume fractions of nearly 100% may be supported using the
appropriate dispersant the choice of which is now very refined and outside the
Scope of this Guide. As a general point low HLB dispersants are used to support
water-in-oil (HLB number 5 or less). Dispersants, with HLB 7 to 16 are preferred
for oil-in-water.
6.2.2 'Hold-Up' (Dispersed Phase Volume Fraction) and Impeller Position
In the absence of dispersants these parameters have the major effect. The
phase of less than 40% volume fraction is likely to be dispersed. Mounting the
impeller in a phase favors the dispersion of the opposite phase so that up to 60%
of the opposite phase may be dispersed in a batch operation by mounting the
impeller in a particular phase.
6.3
Design for Mass Transfer
6.3.1 Operating Speed
It is recommended that the impeller be operated at the power levels indicated by
equations 3 and 4, since mass transfer rates will generally be high compared to
rates of reaction.
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9. 6.3.2 Scale-Up
Scale-up of the recommended geometry at constant (P/V) from 20 liters
laboratory vessels is preferred as it is not possible to define the effect of
interfacial properties on droplet coalescence, hence equilibrium droplet size
distribution. In polymerization reactors, for example, it will also be easier and
more accurate to adopt this empirical approach than to attempt to predict solute
diffusivities and distribution coefficients over the whole process.
6.3.3 Prediction of Interfacial Area
The correlation:
is recommended for an estimate of the mean droplet diameter and interfacial
area per unit dispersion volume in diagnostic work, or in relatively simple
systems such as washers.
Note the constant in equation 5 is dimensionless.
6.3.4 Prediction of Mass Transfer Coefficients
Inside Drop:
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10. Outside drop:
where Dd and Dc are the dispersed and continuous phase diffusivities.
These expressions are strictly appropriate to non coalescing systems, but will
give general order of magnitude estimates. Note that kL is generally greater than
kd and the choice of dispersed phase may be significant.
6.4 Design for Dispersed Phase Mixing
Collision frequency increases according to (P/V) to the 0.4 power. Detailed
predictions are even more limited than those on mass transfer and empirical
tests are indicated.
6.5 Hold-Up in Continuous Vessels
The vessel outflow is not usually extracted isokinetically so that the ratio of
phases inside the vessel is not necessarily the same as that in the feed. In scale
up work ensure that the ratio:
(where v is the fluid velocity in the outflow) is the same as that proposed on the
full scale design.
7
FLOW MIXERS
Flow in the flow mixers can be laminar or turbulent; the transition Reynolds
number ranges are given in Table 1. The Sulzer SMV mixer is recommended by
Sulzer for Re > 200, for Re at or below 200 the SMX mixer should be used.
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11. TABLE 1
7.1
REYNOLDS NUMBER RANGES
Design for Turbulent Conditions
Flow mixers operate under plug-glow conditions; this contributes to the high
volumetric and power efficiencies although their ability to generate very high
levels of turbulence, which dissipate extremely high power per unit volume (up to
700 kW/m 3) is also important.
With immiscible liquid systems they are best employed in a continuous process
requiring less than 100 seconds to complete the required operation (e.g. mass
transfer, chemical reaction). Accurate metering of the two liquid streams to the
mixer may be needed, possibly calling for expensive flow control equipment.
One advantage of continuous flow mixers is that they readily couple to
hydrocylcone phase separators, via in-line coalescers if necessary.
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12. 7.1.1 Recommended Configurations
At present there is no evidence that one sort of flow mixer is more efficient than
another in using energy to promote liquid-liquid processes such as droplet breakup and mass transfer. Conventional column packings seem to perform as
effectively as the proprietary devices. The simple design of the Kenics mixer
makes for easy cleaning while the Sulzer mixers will be shorter for a given
pressure drop.
7.1.2 Pressure Drop and Power Dissipation
The frictional forces between the flowing liquid and the flow mixer lead to
turbulence, power dissipation and pressure drop and to droplet break-up and
promotion of mass transfer between the phases.
For the calculation of pressure drop and power dissipation, refer to GBHE-PEGMIX-701, Clause 7 for static mixers in miscible liquid systems. Use the mixed
density and viscosity values as calculated by equations 1 and 2.
7.1.3 Design for Mass Transfer
The design methods for mass transfer operations in immiscible liquid-liquid
systems apply to all systems where physical mass transfer is the limiting
process. It thus includes systems where a fast chemical reaction which is not rate
limiting is occurring simultaneously with mass transfer.
For systems which do not coalesce very readily, the values of KLa for a given
power per unit volume can be enhanced by interposing empty pipe between the
mixer elements or groups of elements. No specific guidelines are available;
experiments with the system being used are essential.
The coalescence and separation of the phases after mass transfer should also
be studied experimentally prior to the design of the full-scale unit. The droplet
size achieved in the flow mixer is a compromise to give the optimum combination
of mass transfer rates and settling rates in terms of equipment size and cost. The
following points relate to the phase separation:
(a)
flow mixers give a narrower range of droplet sizes than stirred tanks; the
absence of very small droplets reduces overall settling times;
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13. (b)
settling times increase with the flow rate through the mixer due to the
decrease in droplet size with increasing flow rate;
(c)
when the organic phase is continuous, electrostatic methods of
accelerating separation can be used;
(d)
in-line coalescers using 'Knitmesh' packing of appropriate material can
improve the settling performance;
(e)
settling time is extremely sensitive to the presence of traces of impurities
at concentrations too small to affect the measured interfacial tension. It is
therefore important that, whenever possible, the liquids used in the
laboratory study should have the same contaminants and impurity levels
as the plant process liquids. Quick comparative checks of settling times
can be made by following Rushton's method (Chem.Eng. Prog., 52, 515, 1956). This involves producing a complete emulsion, then stopping the
impeller and noting the time for the dispersion to settle to the first
appearance of a clear interface.
(f)
Water-in-oil (W/O) dispersions generally settle much faster than the oil-inwater (O/W) dispersions formed by the same two liquids.
Control over which phase becomes dispersed is important because this can
affect mass transfer and settling performance. The material of construction of the
flow mixer should be chosen so that it is wet more easily by the liquid required to
be the continuous phase. Thus polypropylene might be used if an organiccontinuous system were required. (Polypropylene 'Intalox' saddles form an
effective flow mixer packing.) The liquid forming the larger proportion of the total
feed is also more likely to form the continuous phase although dispersions with
over 90% by volume of the dispersed phase can be made.
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14. K La values are obtained from steady state experiments using the relation:
A plot of KLa vs P/V of the form
as in Figure 2 is likely to be obtained, where C is a constant for the particular
liquid-liquid system concerned, dependent on the value of f and the flow regime,
but not on the scale of the equipment. n is likely to be in the range 0.5 to 1.0.
The calculation procedure is as follows:
(1)
a possible design is selected in terms of diameter, flow rate and number of
elements;
(2)
the P/V is calculated as recommended in 7.1.2;
(3)
obtain KLa from an experimental plot of KLa vs P/V;
(4)
E is calculated from equation 8;
(5)
further designs are examined to arrive at the most suitable one, taking into
account the settling and post-contacting re-coalescence.
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15. In order to allow for design uncertainties, including that attached to KLa, the
length of the mixer should be 30% longer than the calculated design value.
FIGURE 2 EXPERIMENTAL RELATIONSHIP BETWEEN MASS TRANSFER
COEFFICIENT AND POWER DENSITY
Figure 2 shows the relationship between Mass Transfer coefficient, KLa, and
Power Density, P/V, in flow mixers and stirred tanks for the extraction of Cu++
from aqueous solutions using chelating agents in hydrocarbons.
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16. 7.1.4 Design for Specified Droplet Size
Design to a specified droplet size may be useful, for instance, in preparing a
dispersion of a monomer in water prior to polymerization. It is recommended that
a minimum of five flow mixer elements are used to control droplet size. When
considering a flow mixer system for a process requiring a specified droplet size it
is very important to identify the variable(s) and the control method which will be
used for fine-tuning the system. Design calculations should be carried out with
this in mind.
The design equations for calculating the Sauter mean droplet diameter, dsy , with
liquids of equal viscosity under conditions of low coalescence are:
A more detailed design procedure for static mixers to produce a required drop
size has been developed by Middleton.
When coalescence is significant, which may be the case for systems where the
volume fraction of the dispersed phase is greater than 0.1, the predicted values
of dsv may be low.
The design equation for calculating dsv for two low viscosity (µ - 10-3 N s/m2)
immiscible liquids flowing in a straight empty pipe of diameter D t is:
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17. A pipe length of 200-500 diameters is necessary to achieve droplets of this
limiting size.
For a helical coil, the equation to be used is:
As equation (13) has only been tested for Dt / DH = 0.08 and a helix angle of 6°,
the range of validity is uncertain.
Orifice plates and valves can be used as flow mixers for immiscible liquids
though their efficiencies are said to be lower than that of a properly designed flow
mixer. For a single orifice mounted centrally in a tube, receiving a jet of the
dispersing liquid, the following dimensional equation (requiring the use of SI units
) may be used with caution to calculate the Sauter mean droplet diameter in m,
provided the variables are within the range tested:
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18. The use of equation (12) for calculating drop sizes in full scale equipment
requires extreme caution but may give useful rough equipment sizing from which
the required drop size can be obtained by tuning the system: adjusting flow rate,
orifice size or interfacial tension.
7.2
Design for Laminar Conditions
Liquid-liquid dispersion in flow mixers under laminar conditions is likely to be
used in polymer melt processing for mixing in additives, either in a solvent or as a
master batch in polymer. Occasionally two-phase mixtures of immiscible
polymers are made because of their particular properties. This clause also
covers the problem of dispersing a relatively small amount (up to 20%) of a low
viscosity into a high viscosity liquid, and vice versa, whether or not the two are
ultimately miscible.
The design procedure in the GBHE Mixing and Agitation Manual is derived from
the account given by an American Company (1982). It is so far unproven and
should therefore be used with caution. It is strongly recommended that a smallscale experimental study of the two-liquid system involved be carried out. The
American Company only provides information on the Kenics mixer, while
Middleton (1984) gives a design procedure for Sulzer and Kenics mixers.
The American Company defines a reduced shear stress as :
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19. In simple shear fields droplet break-up will occur if SB exceeds a critical value, S
crit of about 0.6 for values of p in the range 0.1 to 1.0. At higher values of p, S crit
increases very rapidly and break-up will not take place at all if p exceeds about
3.0. At values of p below 0.1, S crit is given by:
The American Company indicates that this relationship applies down to p = 3 *
10-6 but note that other Authors have reached somewhat different conclusions,
perhaps because of the low values of oc in their work. The American Company
also provides information on the effect of subjecting a droplet to a reduced shear
much greater than the critical value. The time required for break-up decreases
rapidly and the number of fragments increases from 10 - 30 at the critical value to
over 1000 at 10 times the critical reduced shear stress.
In extensional shear fields there is again a critical value of SB which must be
exceeded for break-up to occur, again S crit depends on p, having a minimum
value of 0.2 at p = 5 and rising to 0.5 at p = 1000, according to the relation:
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20. DOCUMENTS REFERRED TO IN THIS PROCESS ENGINEERING GUIDE
This Process Engineering Guide makes reference to the following documents:
GBHE ENGINEERING GUIDES
Glossary of Engineering Terms
GBHE-PEG-MIX-701
Mixing of Miscible Liquids (referred to in 7.1.2)
GBHE-PEG-MIX-709
High Shear Mixers (referred to in 4.3)
OTHER GBHE DOCUMENTS
GBH Enterprises
Mixing and Agitation Manual (referred to in 7.2).
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21. Refinery Process Stream Purification Refinery Process Catalysts Troubleshooting Refinery Process Catalyst Start-Up / Shutdown
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