Light-Induced Controlled Free Radical Polymerization of Methacrylates Using I...Pawan Kumar
A novel visible light mediated catalytic system
based on low cost iron complex, that is, Fe(bpy)3(PF)6 photocatalyst
that initiates and control the free radical polymerization
of methacrylates using ethyl a-bromoisobutyrate (EBriB) as an
initiator and 20 watt LED as light source is developed. The
polymerization is initiated with turning the light on and immediately
terminated by turning the light off. In addition, the
molecular weight of polymer can be varied by changing the
ratio of monomer and initiator. The merits of the present methodology
lie in the use of low cost less precious, highly abundant
iron-based photocatalyst, avoidance of sacrificial donor
and need of lower catalyst amount under visible light. The
optimum amount of catalyst and initiator were established and
successful polymerization of various methacrylates was
achieved under the optimized polymerization conditions.
The TOTSUCAT technology for catalyst preactivation will allow for fast an hassle free startup with elimination of common phenomena such as exotherms, water make, hydrogen consumption limitations and excessive H2S partial pressure in the system
Light-Induced Controlled Free Radical Polymerization of Methacrylates Using I...Pawan Kumar
A novel visible light mediated catalytic system
based on low cost iron complex, that is, Fe(bpy)3(PF)6 photocatalyst
that initiates and control the free radical polymerization
of methacrylates using ethyl a-bromoisobutyrate (EBriB) as an
initiator and 20 watt LED as light source is developed. The
polymerization is initiated with turning the light on and immediately
terminated by turning the light off. In addition, the
molecular weight of polymer can be varied by changing the
ratio of monomer and initiator. The merits of the present methodology
lie in the use of low cost less precious, highly abundant
iron-based photocatalyst, avoidance of sacrificial donor
and need of lower catalyst amount under visible light. The
optimum amount of catalyst and initiator were established and
successful polymerization of various methacrylates was
achieved under the optimized polymerization conditions.
The TOTSUCAT technology for catalyst preactivation will allow for fast an hassle free startup with elimination of common phenomena such as exotherms, water make, hydrogen consumption limitations and excessive H2S partial pressure in the system
Study and Implementation of Advanced Control and Optimization for Ethylene Fu...idescitation
This paper relates to study of advanced control and
optimization of Ethylene furnace by using Model Predictive
Control Professional (MPCPro) block of deltaV system and
also some efforts are made for Implementation of severity
control for part of Ethylene Furnace. Control and optimization
of Ethylene Furnace is designed for MPCPro block, built in
deltaV control studio. This software package consist of large
number of control modules.
Model of severity control for process zone-2 is developed
for process with regulatory loops and this model is further
used in MPCPro block of deltaV system. Control is generated
using new control definition and then we verify the
performance of process for PID control and for MPC at
supervisory level with regulatory loops. The objective behind
using MPC is there are 4 main challenges to restrict the
process for maximum formation of ethylene are short
residence time, controlled pressure, controlled temperature,
steam to hydrocarbon ratio. The process is also get affected by
the disturbances like Fuel BTU, Feed inlet temperature these
issues are get registered while using MPC
Temperature excursions in hydrogenation reactors may have several causes, the most common ones being:-
i) Loss of recycle quench system. This could be either the liquid or gas stream. The condition is made worse if the make-up gas keeps flowing.
ii) Excessive temperatures. The loss of cooling medium ........
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
Naphtha Steam Reforming Catalyst Reduction with MethanolGerard B. Hawkins
Procedure for Naphtha Steam Reforming Catalyst Reduction with Methanol
Scope
This procedure applies to the in situ reduction of VULCAN Series steam reforming catalysts using methanol cracking to form hydrogen over the catalyst in the steam reformer.
The procedure is likely to be applied to plants using only heavier feeds (e.g.: LPG and/or naphtha) and some combination of VULCAN Series catalysts.
Introduction
A small number of steam reforming plants do not have an available source of the commonly used reducing media (e.g.: hydrogen, hydrogen-rich off-gas, natural gas). These plants will usually operate on LPG and/or naphtha feed only where cracking of this hydrocarbon is not usually advised for reduction of the steam reforming catalyst ...
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
Low Temperature Shift Catalyst Reduction Procedure
VSG-C111 as supplied contains copper oxide; it is activated for the low temperature shift duty by reducing the copper oxide component to metallic copper with hydrogen. The reaction is highly exothermic. In order to achieve maximum activity, good performance and long life, it is essential that the reduction is conducted under correctly controlled conditions. Great care must be taken to avoid thermal damage during this critical operation.
DEACTIVATION OF METHANOL SYNTHESIS CATALYSTS
CONTENTS
1 INTRODUCTION
2 THERMAL SINTERING
3 CATALYST POISONING
4 REACTANT INDUCED DEACTIVATION
5 SUMMARY
TABLES
1 DEACTIVATION PROCESSES ON METHANOL SYNTHESIS CATALYSTS
2 MELTING POINT, HUTTIG AND TAMMANN TEMPERATURES OF COPPER, IRON AND NICKEL
3 SINTERING RATE CONSTANTS CALCULATED INLET AND OUTLET SIDE STREAM UNIT FOR VULCAN VSG-M101
4 COMPARISON BETWEEN CALCULATED S∞ AND DISCHARGED MEASUREMENTS ON VULCAN VSG-M101
5 EFFECT OF POSSIBLE CONTAMINANTS AND POISONS ON CU/ZNO/AL2O3 CATALYSTS FOR METHANOL SYNTHESIS
6 GUARD SCREENING TEST RESULTS ON METHANOL MICRO-REACTOR. EFFECT OF DEPOSITED METALS ON METHANOL ACTIVITY
FIGURES
1 THE HΫTTIG AND TAMMANN TEMPERATURES OF THE COMPONENTS OF A SYNTHESIS CATALYST
2 A SCHEMATIC REPRESENTATION OF TWO CATALYST SINTERING MECHANISMS
3 SIDE STREAM DATA FOR VULCAN VSG-M101. INLET TEMPERATURE 242 OC, PRESSURE 1500 PSI, GAS COMPOSITION 6% CO, 9.2% CO2, 66.9% H2, 2.5% N2 AND 15.4% CH4, SPACE VELOCITY 17,778 HR-1. MEAN OUTLET TEMPERATURE 280 OC
4 TEMPERATURE DEPENDENCE OF THE RATE OF SINTERING
5 MECHANISM OF SULFUR RETENTION
6 CORRELATION OF SULFUR CAPACITY WITH TOTAL SURFACE AREA
7 EFFECT OF DEPOSITED (NI+FE) PPM ON METHANOL SYNTHESIS CATALYST ACTIVITY
8 DISCHARGED (FE + NI) DEPOSITION LEVELS ON METHANOL SYNTHESIS PLANT SAMPLES
9 EPMA ANALYSIS OF DISCHARGED LABORATORY SAMPLE OF POISONED VULCAN VSG-M101
10 THE EFFECT OF CO2 ON SYNTHESIS CATALYST DEACTIVATION
REFERENCES
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
Pumps for Hydrocarbon Service
1 SCOPE
2 HYDROCARBON PROPERTIES
2.1 General
2.2 Pure Hydrocarbons
2.3 Associated Compounds
2.4 Crude Oil
2.5 Toxicology
2.6 Cavitation
2.7 Velocity of Sound
3 FLAMMABILITY HAZARDS
3.1 General
3.2 Definitions
3.3 The Electrical Area Classification
4 CHOICE OF PUMP TYPE
5 LINE DIAGRAM (PROCESS)
6 LAYOUT
7 SHAFT SEALS
7.1 Selection
7.2 Engineering of Seals
8 CONSTRUCTION FEATURES
8.1 General
8.2 Effects of Low Density
9 MATERIALS OF CONSTRUCTION
9.1 Process Wetted Parts
9.2 Mechanical Components
9.3 Non Metallic’s
APPENDIX A - BARNARD & WEIR SEAL THEORY FIGURES
1 VAPOR PRESSURE OF HYDROCARBONS
2 VAPOR PRESSURE OF LIGHT HYDROCARBONS
3 VAPOR PRESSURE OF GASOLINES
4 SPECIFIC HEAT OF HYDROCARBON LIQUIDS
5 SPECIFIC GRAVITY OF OLEFINE, DI OLEFINES AND PARAFFINS
6 SPECIFIC GRAVITY OF AROMATICS
7 VISCOSITY - TEMPERATURE CHART FOR PARAFFINS, AROMATICS
AND PETROLEUM FRACTIONS
8 VISCOSITY - TEMPERATURE CHART FOR MINERAL LUBRICATING
OILS
TABLES
1 PURE HYDROCARBON PROPERTIES
2A CRUDE OILS PROPERTIES
2B NINIAN: PROPERTIES OF CRUDE OIL, NAPHTHAS AND KEROSENE
2C NINIAN: PROPERTIES OF GAS OILS AND RESIDUES
3 PURE HYROCARBON FLAMMABILITY PROPERTIES
BIBLIOGRAPHY
H - Acid Caustic Fusion Stage
CONTENTS
0 INTRODUCTION
1 DESIGN INFORMATION
1.1 Reactor Type
1.2 Temperature Range
1.3 Pressure Range
1.4 Chemical System
2 BACKGROUND
3 KINETICS AND MECHANISM
4 MAXIMUM YIELD AND IMPLICATIONS FOR REACTOR DESIGN
5 USE OF DESIGN MODEL FOR START-UP AND MANUFACTURING MONITORING
6 BIBLIOGRAPHY
FIGURES
1 FUSION MODEL OUTLINE MECHANISM AND KINETIC SCHEME
2 TEST RUN OPTIMIZATION OF HEATING TIME 3600 kg/h STEAM
Naphtha Steam Reforming Catalyst Reduction by NH3 CrackingGerard B. Hawkins
Procedure for Naphtha Steam Reforming Catalyst Reduction by NH3 Cracking
Scope
This procedure applies to the in situ reduction of VULCAN Series steam reforming catalysts using ammonia cracking to form hydrogen over the catalyst in the steam reformer. This procedure covers plants with a dry gas circulation loop for reduction. The procedure is likely to be applied to plants using only heavier feeds (e.g.: LPG and/or naphtha) and some combination of VULCAN Series catalysts.
Introduction
A small number of steam reforming plants do not have an available source of the commonly used reducing media (e.g.: hydrogen, hydrogen-rich off-gas, natural gas). These plants will usually operate on LPG and/or naphtha feed only where cracking of this hydrocarbon is not usually advised for reduction of the steam reforming catalyst. In such circumstances, the plant may be designed to use the installed steam reforming catalyst to crack ammonia to provide hydrogen for the reformer catalyst reduction....
Heating and Cooling of Batch Processes
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
3.1 units
4 STATEMENT OF THE PROBLEM
5 DEVELOPMENT OF THE METHOD
5.1 Assumptions
5.2 Basic Equations
6 APPLICATION OF THE METHOD
6.1 Determining the Behavior of an Existing System
6.2 Specifying the Heat Transfer Duty for a New System
APPENDICES
A DERIVATION OF THE EQUATIONS
B WORKED EXAMPLES
FIGURES
1 CASES CONSIDERED
High Temperature Shift Catalyst Reduction ProcedureGerard B. Hawkins
High Temperature Shift Catalyst Reduction Procedure
The catalyst, as supplied, is Fe2O3. This reduces to the active form, Fe3O4, in the presence of hydrogen when process gas is admitted to the reactor.
1. The mildly exothermic reactions are:
3 Fe2O3 + H2 ========= 2 Fe3O4 + H2O
3 Fe2O3 + CO ========= 2 Fe3O4 + CO2
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
Determination of Carbon Dioxide, Ethane And Nitrogen in Natural Gas by Gas C...Gerard B. Hawkins
Determination of Carbon Dioxide, Ethane
And Nitrogen in Natural Gas by Gas Chromatography
1 SCOPE AND FIELD OF APPLICATION
This document is a method for the determination of carbon dioxide, ethane and nitrogen in natural gas in the range 0-10% v/v.
2 PRINCIPLE
The gas sample will be injected automatically by a ten port valve onto the poraplot U column. The nitrogen will elute first and be switched to the mole sieve column. The mole sieve column will be isolated and the poraplot column will elute the carbon dioxide and ethane via a restrictor column to the detector. After the elution of the carbon dioxide and ethane the poraplot column will be back flushed. Then the nitrogen will be allowed to elute from the mole sieve column (see figure 1.) ...
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
Slack (or Teams) Automation for Bonterra Impact Management (fka Social Soluti...Jeffrey Haguewood
Sidekick Solutions uses Bonterra Impact Management (fka Social Solutions Apricot) and automation solutions to integrate data for business workflows.
We believe integration and automation are essential to user experience and the promise of efficient work through technology. Automation is the critical ingredient to realizing that full vision. We develop integration products and services for Bonterra Case Management software to support the deployment of automations for a variety of use cases.
This video focuses on the notifications, alerts, and approval requests using Slack for Bonterra Impact Management. The solutions covered in this webinar can also be deployed for Microsoft Teams.
Interested in deploying notification automations for Bonterra Impact Management? Contact us at sales@sidekicksolutionsllc.com to discuss next steps.
"Impact of front-end architecture on development cost", Viktor TurskyiFwdays
I have heard many times that architecture is not important for the front-end. Also, many times I have seen how developers implement features on the front-end just following the standard rules for a framework and think that this is enough to successfully launch the project, and then the project fails. How to prevent this and what approach to choose? I have launched dozens of complex projects and during the talk we will analyze which approaches have worked for me and which have not.
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Study and Implementation of Advanced Control and Optimization for Ethylene Fu...idescitation
This paper relates to study of advanced control and
optimization of Ethylene furnace by using Model Predictive
Control Professional (MPCPro) block of deltaV system and
also some efforts are made for Implementation of severity
control for part of Ethylene Furnace. Control and optimization
of Ethylene Furnace is designed for MPCPro block, built in
deltaV control studio. This software package consist of large
number of control modules.
Model of severity control for process zone-2 is developed
for process with regulatory loops and this model is further
used in MPCPro block of deltaV system. Control is generated
using new control definition and then we verify the
performance of process for PID control and for MPC at
supervisory level with regulatory loops. The objective behind
using MPC is there are 4 main challenges to restrict the
process for maximum formation of ethylene are short
residence time, controlled pressure, controlled temperature,
steam to hydrocarbon ratio. The process is also get affected by
the disturbances like Fuel BTU, Feed inlet temperature these
issues are get registered while using MPC
Temperature excursions in hydrogenation reactors may have several causes, the most common ones being:-
i) Loss of recycle quench system. This could be either the liquid or gas stream. The condition is made worse if the make-up gas keeps flowing.
ii) Excessive temperatures. The loss of cooling medium ........
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
Naphtha Steam Reforming Catalyst Reduction with MethanolGerard B. Hawkins
Procedure for Naphtha Steam Reforming Catalyst Reduction with Methanol
Scope
This procedure applies to the in situ reduction of VULCAN Series steam reforming catalysts using methanol cracking to form hydrogen over the catalyst in the steam reformer.
The procedure is likely to be applied to plants using only heavier feeds (e.g.: LPG and/or naphtha) and some combination of VULCAN Series catalysts.
Introduction
A small number of steam reforming plants do not have an available source of the commonly used reducing media (e.g.: hydrogen, hydrogen-rich off-gas, natural gas). These plants will usually operate on LPG and/or naphtha feed only where cracking of this hydrocarbon is not usually advised for reduction of the steam reforming catalyst ...
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
Low Temperature Shift Catalyst Reduction Procedure
VSG-C111 as supplied contains copper oxide; it is activated for the low temperature shift duty by reducing the copper oxide component to metallic copper with hydrogen. The reaction is highly exothermic. In order to achieve maximum activity, good performance and long life, it is essential that the reduction is conducted under correctly controlled conditions. Great care must be taken to avoid thermal damage during this critical operation.
DEACTIVATION OF METHANOL SYNTHESIS CATALYSTS
CONTENTS
1 INTRODUCTION
2 THERMAL SINTERING
3 CATALYST POISONING
4 REACTANT INDUCED DEACTIVATION
5 SUMMARY
TABLES
1 DEACTIVATION PROCESSES ON METHANOL SYNTHESIS CATALYSTS
2 MELTING POINT, HUTTIG AND TAMMANN TEMPERATURES OF COPPER, IRON AND NICKEL
3 SINTERING RATE CONSTANTS CALCULATED INLET AND OUTLET SIDE STREAM UNIT FOR VULCAN VSG-M101
4 COMPARISON BETWEEN CALCULATED S∞ AND DISCHARGED MEASUREMENTS ON VULCAN VSG-M101
5 EFFECT OF POSSIBLE CONTAMINANTS AND POISONS ON CU/ZNO/AL2O3 CATALYSTS FOR METHANOL SYNTHESIS
6 GUARD SCREENING TEST RESULTS ON METHANOL MICRO-REACTOR. EFFECT OF DEPOSITED METALS ON METHANOL ACTIVITY
FIGURES
1 THE HΫTTIG AND TAMMANN TEMPERATURES OF THE COMPONENTS OF A SYNTHESIS CATALYST
2 A SCHEMATIC REPRESENTATION OF TWO CATALYST SINTERING MECHANISMS
3 SIDE STREAM DATA FOR VULCAN VSG-M101. INLET TEMPERATURE 242 OC, PRESSURE 1500 PSI, GAS COMPOSITION 6% CO, 9.2% CO2, 66.9% H2, 2.5% N2 AND 15.4% CH4, SPACE VELOCITY 17,778 HR-1. MEAN OUTLET TEMPERATURE 280 OC
4 TEMPERATURE DEPENDENCE OF THE RATE OF SINTERING
5 MECHANISM OF SULFUR RETENTION
6 CORRELATION OF SULFUR CAPACITY WITH TOTAL SURFACE AREA
7 EFFECT OF DEPOSITED (NI+FE) PPM ON METHANOL SYNTHESIS CATALYST ACTIVITY
8 DISCHARGED (FE + NI) DEPOSITION LEVELS ON METHANOL SYNTHESIS PLANT SAMPLES
9 EPMA ANALYSIS OF DISCHARGED LABORATORY SAMPLE OF POISONED VULCAN VSG-M101
10 THE EFFECT OF CO2 ON SYNTHESIS CATALYST DEACTIVATION
REFERENCES
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
Pumps for Hydrocarbon Service
1 SCOPE
2 HYDROCARBON PROPERTIES
2.1 General
2.2 Pure Hydrocarbons
2.3 Associated Compounds
2.4 Crude Oil
2.5 Toxicology
2.6 Cavitation
2.7 Velocity of Sound
3 FLAMMABILITY HAZARDS
3.1 General
3.2 Definitions
3.3 The Electrical Area Classification
4 CHOICE OF PUMP TYPE
5 LINE DIAGRAM (PROCESS)
6 LAYOUT
7 SHAFT SEALS
7.1 Selection
7.2 Engineering of Seals
8 CONSTRUCTION FEATURES
8.1 General
8.2 Effects of Low Density
9 MATERIALS OF CONSTRUCTION
9.1 Process Wetted Parts
9.2 Mechanical Components
9.3 Non Metallic’s
APPENDIX A - BARNARD & WEIR SEAL THEORY FIGURES
1 VAPOR PRESSURE OF HYDROCARBONS
2 VAPOR PRESSURE OF LIGHT HYDROCARBONS
3 VAPOR PRESSURE OF GASOLINES
4 SPECIFIC HEAT OF HYDROCARBON LIQUIDS
5 SPECIFIC GRAVITY OF OLEFINE, DI OLEFINES AND PARAFFINS
6 SPECIFIC GRAVITY OF AROMATICS
7 VISCOSITY - TEMPERATURE CHART FOR PARAFFINS, AROMATICS
AND PETROLEUM FRACTIONS
8 VISCOSITY - TEMPERATURE CHART FOR MINERAL LUBRICATING
OILS
TABLES
1 PURE HYDROCARBON PROPERTIES
2A CRUDE OILS PROPERTIES
2B NINIAN: PROPERTIES OF CRUDE OIL, NAPHTHAS AND KEROSENE
2C NINIAN: PROPERTIES OF GAS OILS AND RESIDUES
3 PURE HYROCARBON FLAMMABILITY PROPERTIES
BIBLIOGRAPHY
H - Acid Caustic Fusion Stage
CONTENTS
0 INTRODUCTION
1 DESIGN INFORMATION
1.1 Reactor Type
1.2 Temperature Range
1.3 Pressure Range
1.4 Chemical System
2 BACKGROUND
3 KINETICS AND MECHANISM
4 MAXIMUM YIELD AND IMPLICATIONS FOR REACTOR DESIGN
5 USE OF DESIGN MODEL FOR START-UP AND MANUFACTURING MONITORING
6 BIBLIOGRAPHY
FIGURES
1 FUSION MODEL OUTLINE MECHANISM AND KINETIC SCHEME
2 TEST RUN OPTIMIZATION OF HEATING TIME 3600 kg/h STEAM
Naphtha Steam Reforming Catalyst Reduction by NH3 CrackingGerard B. Hawkins
Procedure for Naphtha Steam Reforming Catalyst Reduction by NH3 Cracking
Scope
This procedure applies to the in situ reduction of VULCAN Series steam reforming catalysts using ammonia cracking to form hydrogen over the catalyst in the steam reformer. This procedure covers plants with a dry gas circulation loop for reduction. The procedure is likely to be applied to plants using only heavier feeds (e.g.: LPG and/or naphtha) and some combination of VULCAN Series catalysts.
Introduction
A small number of steam reforming plants do not have an available source of the commonly used reducing media (e.g.: hydrogen, hydrogen-rich off-gas, natural gas). These plants will usually operate on LPG and/or naphtha feed only where cracking of this hydrocarbon is not usually advised for reduction of the steam reforming catalyst. In such circumstances, the plant may be designed to use the installed steam reforming catalyst to crack ammonia to provide hydrogen for the reformer catalyst reduction....
Heating and Cooling of Batch Processes
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
3.1 units
4 STATEMENT OF THE PROBLEM
5 DEVELOPMENT OF THE METHOD
5.1 Assumptions
5.2 Basic Equations
6 APPLICATION OF THE METHOD
6.1 Determining the Behavior of an Existing System
6.2 Specifying the Heat Transfer Duty for a New System
APPENDICES
A DERIVATION OF THE EQUATIONS
B WORKED EXAMPLES
FIGURES
1 CASES CONSIDERED
High Temperature Shift Catalyst Reduction ProcedureGerard B. Hawkins
High Temperature Shift Catalyst Reduction Procedure
The catalyst, as supplied, is Fe2O3. This reduces to the active form, Fe3O4, in the presence of hydrogen when process gas is admitted to the reactor.
1. The mildly exothermic reactions are:
3 Fe2O3 + H2 ========= 2 Fe3O4 + H2O
3 Fe2O3 + CO ========= 2 Fe3O4 + CO2
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
Determination of Carbon Dioxide, Ethane And Nitrogen in Natural Gas by Gas C...Gerard B. Hawkins
Determination of Carbon Dioxide, Ethane
And Nitrogen in Natural Gas by Gas Chromatography
1 SCOPE AND FIELD OF APPLICATION
This document is a method for the determination of carbon dioxide, ethane and nitrogen in natural gas in the range 0-10% v/v.
2 PRINCIPLE
The gas sample will be injected automatically by a ten port valve onto the poraplot U column. The nitrogen will elute first and be switched to the mole sieve column. The mole sieve column will be isolated and the poraplot column will elute the carbon dioxide and ethane via a restrictor column to the detector. After the elution of the carbon dioxide and ethane the poraplot column will be back flushed. Then the nitrogen will be allowed to elute from the mole sieve column (see figure 1.) ...
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
Similar to Eurecat palladium catalyst reactivation (20)
Slack (or Teams) Automation for Bonterra Impact Management (fka Social Soluti...Jeffrey Haguewood
Sidekick Solutions uses Bonterra Impact Management (fka Social Solutions Apricot) and automation solutions to integrate data for business workflows.
We believe integration and automation are essential to user experience and the promise of efficient work through technology. Automation is the critical ingredient to realizing that full vision. We develop integration products and services for Bonterra Case Management software to support the deployment of automations for a variety of use cases.
This video focuses on the notifications, alerts, and approval requests using Slack for Bonterra Impact Management. The solutions covered in this webinar can also be deployed for Microsoft Teams.
Interested in deploying notification automations for Bonterra Impact Management? Contact us at sales@sidekicksolutionsllc.com to discuss next steps.
"Impact of front-end architecture on development cost", Viktor TurskyiFwdays
I have heard many times that architecture is not important for the front-end. Also, many times I have seen how developers implement features on the front-end just following the standard rules for a framework and think that this is enough to successfully launch the project, and then the project fails. How to prevent this and what approach to choose? I have launched dozens of complex projects and during the talk we will analyze which approaches have worked for me and which have not.
GraphRAG is All You need? LLM & Knowledge GraphGuy Korland
Guy Korland, CEO and Co-founder of FalkorDB, will review two articles on the integration of language models with knowledge graphs.
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https://arxiv.org/abs/2306.08302
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State of ICS and IoT Cyber Threat Landscape Report 2024 previewPrayukth K V
The IoT and OT threat landscape report has been prepared by the Threat Research Team at Sectrio using data from Sectrio, cyber threat intelligence farming facilities spread across over 85 cities around the world. In addition, Sectrio also runs AI-based advanced threat and payload engagement facilities that serve as sinks to attract and engage sophisticated threat actors, and newer malware including new variants and latent threats that are at an earlier stage of development.
The latest edition of the OT/ICS and IoT security Threat Landscape Report 2024 also covers:
State of global ICS asset and network exposure
Sectoral targets and attacks as well as the cost of ransom
Global APT activity, AI usage, actor and tactic profiles, and implications
Rise in volumes of AI-powered cyberattacks
Major cyber events in 2024
Malware and malicious payload trends
Cyberattack types and targets
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Attacks on counties – USA
Expansion of bot farms – how, where, and why
In-depth analysis of the cyber threat landscape across North America, South America, Europe, APAC, and the Middle East
Why are attacks on smart factories rising?
Cyber risk predictions
Axis of attacks – Europe
Systemic attacks in the Middle East
Download the full report from here:
https://sectrio.com/resources/ot-threat-landscape-reports/sectrio-releases-ot-ics-and-iot-security-threat-landscape-report-2024/
Let's dive deeper into the world of ODC! Ricardo Alves (OutSystems) will join us to tell all about the new Data Fabric. After that, Sezen de Bruijn (OutSystems) will get into the details on how to best design a sturdy architecture within ODC.
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:
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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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Charlie Greenberg, Host
Epistemic Interaction - tuning interfaces to provide information for AI supportAlan Dix
Paper presented at SYNERGY workshop at AVI 2024, Genoa, Italy. 3rd June 2024
https://alandix.com/academic/papers/synergy2024-epistemic/
As machine learning integrates deeper into human-computer interactions, the concept of epistemic interaction emerges, aiming to refine these interactions to enhance system adaptability. This approach encourages minor, intentional adjustments in user behaviour to enrich the data available for system learning. This paper introduces epistemic interaction within the context of human-system communication, illustrating how deliberate interaction design can improve system understanding and adaptation. Through concrete examples, we demonstrate the potential of epistemic interaction to significantly advance human-computer interaction by leveraging intuitive human communication strategies to inform system design and functionality, offering a novel pathway for enriching user-system engagements.
Search and Society: Reimagining Information Access for Radical FuturesBhaskar Mitra
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Topics covered:
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Pradeep Chinnala, Senior Consultant Automation Developer @WonderBotz and UiPath MVP
Deepak Rai, Automation Practice Lead, Boundaryless Group and UiPath MVP
UiPath Test Automation using UiPath Test Suite series, part 4DianaGray10
Welcome to UiPath Test Automation using UiPath Test Suite series part 4. In this session, we will cover Test Manager overview along with SAP heatmap.
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1. Insights into SAP testing best practices
2. Heatmap utilization for testing
3. Optimization of testing processes
4. Demo
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Execution from the test manager
Orchestrator execution result
Defect reporting
SAP heatmap example with demo
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UiPath Test Automation using UiPath Test Suite series, part 4
Eurecat palladium catalyst reactivation
1. Reactivation of
Palladium Catalysts
Through extensive R&D efforts, Eurecat has developed a novel method to recover the activity
of spent palladium catalysts. This technology, called Reactivation, involves a multi-step proc-
ess that identifies and carefully removes the contaminants causing deactivation of the cata-
lyst. After treatment with Reactivation, a high performance catalyst can be returned to the cus-
tomer with activity that often approaches the level of fresh catalyst.
Conventional regeneration techniques typically involve exposure of the catalyst to high tem-
peratures under air and/or steam to remove carbon contamination. Our tests have proven that
exothermic treatments such as this almost always lead to sintering of the active palladium
sites, resulting in the permanent loss of catalytic activity. In addition, an “air burn” does little
to remove other catalyst poisons and in fact can permanently bond some otherwise transient
poisons to the active sites.
Eurecat’s Reactivation process is much different than standard regeneration techniques. Each
project begins with a thorough analysis of the spent catalyst to determine the primary deactiva-
tion mechanism and levels of contamination. Once our analysis is complete, a treatment plan
will be developed to regain or tune the desirable catalytic properties . After processing a sample in our pilot
plant, specially developed hydrogenation activity tests are performed to confirm the effectiveness of the pro-
posed treatment plan. Activity test results, including a comparison of the Reactivated catalyst to fresh catalyst,
are presented to the customer for approval prior to processing on the commercial scale (when time allows).
Installed Applications
Chemicals / Petrochemicals Refineries
• Front End Acetylene Hydrogenation • HF Acid Alkylation Pre-treat
• Back End Acetylene Hydrogenation • Sulfuric Acid Alkylation Pre-treat
• MAPD
• First Stage Pygas
Eurecat U.S. Inc Visit us on the web at www.eurecat.com
1331 Gemini, Suite 310 Or send us an email at: info@eurecat.com
Houston, TX 77058
Phone : 281.218.0669
2. Hydro Isom erization Com parison
3.5
As Received Methyl 2-butene
3.0 Fresh Methyl 2-butene
Reactivated Methyl 2-butene
2.5
2.0
Wt%
1.5
1.0
0.5
0.0
0 18 36 54 72 90 108 126 144 162 180 198
Tim e
Above catalyst installed in a refinery for a hydrofluoric acid alkylation pre-treat application. Butadiene
conversion to the more desirable butene-2 was observed in Eurecat testing. The refinery experienced
an octane boost over 2 points in their alkylate when compared to previously installed charges.
Front-end Ethylene Catalyst
Reactivated isoprene Reactivated isopentene Reactivated isopentane
5.5
Reference isoprene Reference isopentene Reference isopentane
5.0
4.5
4.0
3.5
3.0
2.5
2.0
1.5
1.0
0.5
0.0
0.00 18.00 36.00 54.00 72.00 90.00 108.00 126.00 144.00 162.00 180.00
T ime
Front end total raw gas acetylene converter catalyst installed and operating on its 3rd REACTIVATION cy-
cle (2+ years for each cycle).
Catalyst demonstrates superior selectivity and comparable activity to its reference standard and has
demonstrated a wide range of operational stability thus eliminating flaring incidents from hyper-activity.