This presentation covers the process of sizing and scheduling of Gathering Systems, including how to approach challenges by using model development and automation and interpretation of the results. Additionally, we compare between HYSYS Hydraulics and HYSYS Dynamics.
Natural gas condensates can form liquid slugs in transmission lines. This presentation describes alternative modelling strategies to determine slug volumes
This document provides copyright information and technical support contact details for Aspen Technology's HYSYS 2004.2 Dynamic Modeling software. It lists over 200 Aspen product names that are copyrighted and/or trademarked by Aspen Technology. Contact information is provided for Aspen's Online Technical Support Center, phone support, and email support.
Simulation involves examining a problem using software rather than direct experimentation. Various simulation software are available to model processes. Key aspects of process scheme simulation include determining fluid characteristics, predicting well behavior over its lifetime, selecting an appropriate simulator and thermodynamic package, and ensuring safety margins. Simulation allows examination of topics like vapor-liquid equilibrium, equations of state, mass and heat transfer to help design processes and size equipment in compliance with objectives and specifications.
Juan Pablo Hernández presented information on control valve sizing for compressible fluids. Control valves are used to meet process conditions and product quality specifications. Three methods for sizing control valves were compared: hand made calculations, Fisher software, and Aspen Hysys simulation. All three methods produced similar results for the example case of sizing a control valve for superheated steam. However, the Fisher software was identified as the preferred method due to providing reliable sizing in less time compared to hand calculations.
Aspen Plus basic course for Engineers.
Introduction to Process Modeling/Simulation Software.
INDEX:
Course Objectives
Introduction to Aspen Plus
User Interface & Getting Help
Physical Properties
Introduction to Flowsheet
Unit Operation Models
Reporting Results
Case Studies I, II and III
Case Study IV
Conclusion
Basic Tutorial on Aspen HYSYS Dynamics - Process control (Tutorial 3)Hamed Hoorijani
This document provides instructions for simulating a dynamic process using Aspen HYSIS software. The process involves cooling methane feed in a two-phase separator and controlling the separator temperature and pressure. It describes:
1) Defining the feed stream and adding process equipment like the separator and cooler to the flowsheet.
2) Adding transfer functions to model temperature distribution and dead time.
3) Adding controllers to regulate separator conditions and cooler duty.
4) Creating a strip chart to monitor key temperatures over time.
5) Simulating the process dynamically and observing the changes in temperatures.
It also provides steps for simulating the process using a cascade control loop configuration and adjusting controller and transfer
VARIOUS METHODS OF CENTRIFUGAL COMPRESSOR SURGE CONTROLVijay Sarathy
This document discusses four methods of surge control for centrifugal compressors: 1) controlling surge with a simple minimum flow cold bypass between the discharge and suction sides; 2) controlling surge by altering compressor speed to meet discharge pressure requirements; 3) controlling surge by altering inlet guide vanes or compressor speed to reset cold bypass flow; 4) controlling surge by correlating differential pressure across the compressor to reset minimum cold bypass flow.
Natural gas condensates can form liquid slugs in transmission lines. This presentation describes alternative modelling strategies to determine slug volumes
This document provides copyright information and technical support contact details for Aspen Technology's HYSYS 2004.2 Dynamic Modeling software. It lists over 200 Aspen product names that are copyrighted and/or trademarked by Aspen Technology. Contact information is provided for Aspen's Online Technical Support Center, phone support, and email support.
Simulation involves examining a problem using software rather than direct experimentation. Various simulation software are available to model processes. Key aspects of process scheme simulation include determining fluid characteristics, predicting well behavior over its lifetime, selecting an appropriate simulator and thermodynamic package, and ensuring safety margins. Simulation allows examination of topics like vapor-liquid equilibrium, equations of state, mass and heat transfer to help design processes and size equipment in compliance with objectives and specifications.
Juan Pablo Hernández presented information on control valve sizing for compressible fluids. Control valves are used to meet process conditions and product quality specifications. Three methods for sizing control valves were compared: hand made calculations, Fisher software, and Aspen Hysys simulation. All three methods produced similar results for the example case of sizing a control valve for superheated steam. However, the Fisher software was identified as the preferred method due to providing reliable sizing in less time compared to hand calculations.
Aspen Plus basic course for Engineers.
Introduction to Process Modeling/Simulation Software.
INDEX:
Course Objectives
Introduction to Aspen Plus
User Interface & Getting Help
Physical Properties
Introduction to Flowsheet
Unit Operation Models
Reporting Results
Case Studies I, II and III
Case Study IV
Conclusion
Basic Tutorial on Aspen HYSYS Dynamics - Process control (Tutorial 3)Hamed Hoorijani
This document provides instructions for simulating a dynamic process using Aspen HYSIS software. The process involves cooling methane feed in a two-phase separator and controlling the separator temperature and pressure. It describes:
1) Defining the feed stream and adding process equipment like the separator and cooler to the flowsheet.
2) Adding transfer functions to model temperature distribution and dead time.
3) Adding controllers to regulate separator conditions and cooler duty.
4) Creating a strip chart to monitor key temperatures over time.
5) Simulating the process dynamically and observing the changes in temperatures.
It also provides steps for simulating the process using a cascade control loop configuration and adjusting controller and transfer
VARIOUS METHODS OF CENTRIFUGAL COMPRESSOR SURGE CONTROLVijay Sarathy
This document discusses four methods of surge control for centrifugal compressors: 1) controlling surge with a simple minimum flow cold bypass between the discharge and suction sides; 2) controlling surge by altering compressor speed to meet discharge pressure requirements; 3) controlling surge by altering inlet guide vanes or compressor speed to reset cold bypass flow; 4) controlling surge by correlating differential pressure across the compressor to reset minimum cold bypass flow.
Ai Ch E Overpressure Protection Trainingernestvictor
The document provides an overview of overpressure protection and relief system design. It discusses key concepts such as causes of overpressure, applicable codes and standards, the relief system design process, relief device terminology, and methods for determining relief loads from scenarios such as blocked outlets, thermal expansion, external fires, and automatic control failures. The document is intended to educate engineers on important considerations for properly sizing and designing pressure relief systems.
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
This document provides an overview of using HYSYS simulation software to model and analyze chemical processes. It discusses setting up a HYSYS case by adding components, selecting a fluid package, and entering the simulation environment. It also covers defining process units like separators and heat exchangers, specifying stream properties, performing flash calculations, and generating workbooks. The document is intended as an introduction for students to learn the basic functionality of HYSYS through examples of common unit operations.
This document summarizes API STD 521 Part-I, which provides guidance on overpressure protection for refinery equipment. It discusses overpressure causes and protection philosophies. It also lists the minimum recommended contents for relief system designs and flare header calculations. These include analyzing overpressure causes, operating conditions, relief device sizing, and documentation of simulation inputs and outputs. Various overpressure causes are outlined, such as closed outlets, absorbent or cooling failures, accumulation of non-condensables, abnormal heat input, explosions, and depressurizing. Protection measures against these causes like relief valves, rupture disks, and explosion prevention are also mentioned.
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
This document describes gas sweetening processes used to remove acid gases like H2S and CO2 from natural gas. It focuses on chemical absorption processes using alkanolamine solvents like MEA, DGA, DEA, and MDEA in aqueous solutions. The general process involves absorbing acid gases from the feed gas in an absorber column, regenerating the solvent in a regenerator column, and recycling the regenerated solvent. Key unit operations discussed include the absorber, flash drum, amine/amine heat exchanger, regenerator, reboiler, and condenser. Process conditions and equipment details are provided for the typical operation of each unit.
Excel sheet Download Link: https://www.scribd.com/document/385945712/PSV-Sizing-Tool-API-Based-Calc-Sheets
PSV Sizing for Blocked Liquid Discharge Condition
PSV Sizing for Blocked Gas Discharge Condition
PSV Sizing for Fire Case of Liquid Filled Vessel
PSV Sizing for Control Valve Fail Open Case
Relief Valve Sizing for Thermal Expansion
Restriction Orifice Sizing for Gas Flow
Restriction Orifice Sizing for Liquid Flow
Single Phase Flow Line Sizing Tool
Gas Control Valve Sizing Tool
Based on my 8 years of experience in Oil & Gas industry I can claim that you can find here All what you need to know about Valves. This is an introduction to understand more about their:-
- Classification.
- Selection
- Most common Types.
You can find also more at:
http://hassanelbanhawi.com/staticequipment/valves
All the data and the illustrative figures presented here can be found through two reference books:-
ENGINEERING DATA BOOK by Gas Processors Suppliers Association
Process Technology - Equipment and Systems by Charles E. Thomas
Thank you.
PROCESS STORAGE TANK LAH & LAHH LEVEL CALCULATIONVijay Sarathy
The document contains parameters for a process storage tank including a diameter of 14 feet, height of 18 feet, normal liquid level of 6 feet, and pump inflow of 250 USGPM. It details calculations for the liquid alarm high-high level of 14.74 feet based on filling the tank from the overfill level to that point within 15 minutes, and liquid alarm high level of 8.23 feet calculated from filling within 45 minutes.
- The document discusses sizing pressure safety valves (PSVs) for oil and gas facilities.
- It covers PSV types, causes of chattering, and outlines the step-by-step process for sizing calculations including developing relief scenarios, determining required relief areas, and selecting valve sizes.
- Relief scenarios considered include blocked outlets, thermal expansion, tube rupture, gas blow-by, inlet valve failure, and exterior fires. Relief calculations involve assessing single-phase, two-phase, and transient relief situations.
This document discusses flare technology and applications. It begins with an outline and defines a flare as safety equipment used to burn unwanted gases from oil, gas, and chemical plants. It notes that flares ensure safe combustion to prevent explosions. The document then discusses: the widespread use of flares globally; types of flares including utility, steam-assisted, air-assisted, and multi-point ground flares; factors that influence flare design and performance such as gas composition and flow rates; and issues with flaring including emissions and strategies to minimize flaring.
This document discusses separator design and sizing. It describes different separator configurations including horizontal and vertical separators. It also discusses the use of demisters to remove liquid mist. The document outlines how to size separators using parameters like flow rates, pressures, temperatures and physical properties. It presents methods for sizing separators using computer simulations, hand calculations and industry standards. Sample calculations are shown for various separator cases with and without demisters. Design specifications like diameter, length and L/D ratios are compared between the different methods. The summary reiterates the key steps and outcomes of separator sizing.
Pressure Safety Valve Sizing - API 520/521/526Vijay Sarathy
No chemical process facility is immune to the risk of overpressure to avoid dictating the necessity for overpressure protection. For every situation that demands safe containment of process gas, it becomes an obligation for engineers to equally provide pressure relieving and flaring provisions wherever necessary. The levels of protection are hierarchical, starting with designing an inherently safe process to avoid overpressure followed by providing alarms for operators to intervene and Emergency Shutdown provisions through ESD and SIL rated instrumentation. Beyond these design and instrument based protection measures, the philosophy of containment and abatement steps such as pressure relieving devices, flares, physical dikes and Emergency Response Services is employed
This document outlines a continuing education course on overpressure protection and relief system design. The course contents include an introduction to relief systems, applicable codes and standards, the work process for relief system design, relief device terminology, and causes of overpressure and determining relief loads. The presentation provides information on different types of relief devices, relief system discharge configurations, references and codes, and the multi-step design process and required design data. Key relief device terminology is also defined.
Reservoir development plans require dynamic strategies to optimize production. Recovery methods can be initiated at any stage to improve efficiency. It is common for development plans to change over time due to new understanding, performance, constraints, economics or technologies. Screening studies for improved or enhanced oil recovery methods should consider technical feasibility as well as availability of resources and include decision analysis to define robust project options early. Preliminary performance predictions using simple models can help evaluate recovery process potential in a reservoir.
This document discusses simulation of an aspen flare system using Aspen Flare System Analyzer software. It describes defining the composition, flare network scheme, sources such as control valves and pressure safety valves, and scenarios to simulate, such as all relief devices activating. The outcomes of the simulation can be used to design and verify the flare header size and other parameters meet API standards. The simulation aims to size the flare system and verify its performance under different operating conditions.
This document discusses KLM Technology Group, which provides training and consulting services related to process plant equipment and operations. It focuses on training courses for process flares, including an introduction to process flares, advanced flare design/operation/troubleshooting courses, and a syllabus for an advanced flare systems course. The document provides information on flare types (elevated and ground), system components, design factors and considerations, and safety, environmental, and social requirements related to flare system design.
Safety is the most important factor in designing a process system. Some undesired conditions might happen leading to damage in a system. Control systems might be installed to prevent such conditions, but a second safety device is also needed. One kind of safety device which is commonly used in the processing industry is the relief valve. A relief valve is a type of valve to control or limit the pressure in a system by allowing the pressurised fluid to flow out from the system.
Advisian dynamic process simulation capability june 2019Advisian
Dynamic Process Simulation allows the prediction of not only how a system is expected to behave when it is operating at the targeted design point – it is capable of predicting how it will behave when away from its “design point”.
EDG provides worldwide engineering solutions including asset management and optimization services. They have over 500 employees in offices across the US and internationally. Their digital oil field services integrate real-time data and engineering models to help clients plan, develop and manage upstream oil and gas assets. This includes visualization of production data, automated workflows to optimize wells and facilities, and integrated production modeling to estimate system responses and optimize production levels.
Ai Ch E Overpressure Protection Trainingernestvictor
The document provides an overview of overpressure protection and relief system design. It discusses key concepts such as causes of overpressure, applicable codes and standards, the relief system design process, relief device terminology, and methods for determining relief loads from scenarios such as blocked outlets, thermal expansion, external fires, and automatic control failures. The document is intended to educate engineers on important considerations for properly sizing and designing pressure relief systems.
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
This document provides an overview of using HYSYS simulation software to model and analyze chemical processes. It discusses setting up a HYSYS case by adding components, selecting a fluid package, and entering the simulation environment. It also covers defining process units like separators and heat exchangers, specifying stream properties, performing flash calculations, and generating workbooks. The document is intended as an introduction for students to learn the basic functionality of HYSYS through examples of common unit operations.
This document summarizes API STD 521 Part-I, which provides guidance on overpressure protection for refinery equipment. It discusses overpressure causes and protection philosophies. It also lists the minimum recommended contents for relief system designs and flare header calculations. These include analyzing overpressure causes, operating conditions, relief device sizing, and documentation of simulation inputs and outputs. Various overpressure causes are outlined, such as closed outlets, absorbent or cooling failures, accumulation of non-condensables, abnormal heat input, explosions, and depressurizing. Protection measures against these causes like relief valves, rupture disks, and explosion prevention are also mentioned.
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
This document describes gas sweetening processes used to remove acid gases like H2S and CO2 from natural gas. It focuses on chemical absorption processes using alkanolamine solvents like MEA, DGA, DEA, and MDEA in aqueous solutions. The general process involves absorbing acid gases from the feed gas in an absorber column, regenerating the solvent in a regenerator column, and recycling the regenerated solvent. Key unit operations discussed include the absorber, flash drum, amine/amine heat exchanger, regenerator, reboiler, and condenser. Process conditions and equipment details are provided for the typical operation of each unit.
Excel sheet Download Link: https://www.scribd.com/document/385945712/PSV-Sizing-Tool-API-Based-Calc-Sheets
PSV Sizing for Blocked Liquid Discharge Condition
PSV Sizing for Blocked Gas Discharge Condition
PSV Sizing for Fire Case of Liquid Filled Vessel
PSV Sizing for Control Valve Fail Open Case
Relief Valve Sizing for Thermal Expansion
Restriction Orifice Sizing for Gas Flow
Restriction Orifice Sizing for Liquid Flow
Single Phase Flow Line Sizing Tool
Gas Control Valve Sizing Tool
Based on my 8 years of experience in Oil & Gas industry I can claim that you can find here All what you need to know about Valves. This is an introduction to understand more about their:-
- Classification.
- Selection
- Most common Types.
You can find also more at:
http://hassanelbanhawi.com/staticequipment/valves
All the data and the illustrative figures presented here can be found through two reference books:-
ENGINEERING DATA BOOK by Gas Processors Suppliers Association
Process Technology - Equipment and Systems by Charles E. Thomas
Thank you.
PROCESS STORAGE TANK LAH & LAHH LEVEL CALCULATIONVijay Sarathy
The document contains parameters for a process storage tank including a diameter of 14 feet, height of 18 feet, normal liquid level of 6 feet, and pump inflow of 250 USGPM. It details calculations for the liquid alarm high-high level of 14.74 feet based on filling the tank from the overfill level to that point within 15 minutes, and liquid alarm high level of 8.23 feet calculated from filling within 45 minutes.
- The document discusses sizing pressure safety valves (PSVs) for oil and gas facilities.
- It covers PSV types, causes of chattering, and outlines the step-by-step process for sizing calculations including developing relief scenarios, determining required relief areas, and selecting valve sizes.
- Relief scenarios considered include blocked outlets, thermal expansion, tube rupture, gas blow-by, inlet valve failure, and exterior fires. Relief calculations involve assessing single-phase, two-phase, and transient relief situations.
This document discusses flare technology and applications. It begins with an outline and defines a flare as safety equipment used to burn unwanted gases from oil, gas, and chemical plants. It notes that flares ensure safe combustion to prevent explosions. The document then discusses: the widespread use of flares globally; types of flares including utility, steam-assisted, air-assisted, and multi-point ground flares; factors that influence flare design and performance such as gas composition and flow rates; and issues with flaring including emissions and strategies to minimize flaring.
This document discusses separator design and sizing. It describes different separator configurations including horizontal and vertical separators. It also discusses the use of demisters to remove liquid mist. The document outlines how to size separators using parameters like flow rates, pressures, temperatures and physical properties. It presents methods for sizing separators using computer simulations, hand calculations and industry standards. Sample calculations are shown for various separator cases with and without demisters. Design specifications like diameter, length and L/D ratios are compared between the different methods. The summary reiterates the key steps and outcomes of separator sizing.
Pressure Safety Valve Sizing - API 520/521/526Vijay Sarathy
No chemical process facility is immune to the risk of overpressure to avoid dictating the necessity for overpressure protection. For every situation that demands safe containment of process gas, it becomes an obligation for engineers to equally provide pressure relieving and flaring provisions wherever necessary. The levels of protection are hierarchical, starting with designing an inherently safe process to avoid overpressure followed by providing alarms for operators to intervene and Emergency Shutdown provisions through ESD and SIL rated instrumentation. Beyond these design and instrument based protection measures, the philosophy of containment and abatement steps such as pressure relieving devices, flares, physical dikes and Emergency Response Services is employed
This document outlines a continuing education course on overpressure protection and relief system design. The course contents include an introduction to relief systems, applicable codes and standards, the work process for relief system design, relief device terminology, and causes of overpressure and determining relief loads. The presentation provides information on different types of relief devices, relief system discharge configurations, references and codes, and the multi-step design process and required design data. Key relief device terminology is also defined.
Reservoir development plans require dynamic strategies to optimize production. Recovery methods can be initiated at any stage to improve efficiency. It is common for development plans to change over time due to new understanding, performance, constraints, economics or technologies. Screening studies for improved or enhanced oil recovery methods should consider technical feasibility as well as availability of resources and include decision analysis to define robust project options early. Preliminary performance predictions using simple models can help evaluate recovery process potential in a reservoir.
This document discusses simulation of an aspen flare system using Aspen Flare System Analyzer software. It describes defining the composition, flare network scheme, sources such as control valves and pressure safety valves, and scenarios to simulate, such as all relief devices activating. The outcomes of the simulation can be used to design and verify the flare header size and other parameters meet API standards. The simulation aims to size the flare system and verify its performance under different operating conditions.
This document discusses KLM Technology Group, which provides training and consulting services related to process plant equipment and operations. It focuses on training courses for process flares, including an introduction to process flares, advanced flare design/operation/troubleshooting courses, and a syllabus for an advanced flare systems course. The document provides information on flare types (elevated and ground), system components, design factors and considerations, and safety, environmental, and social requirements related to flare system design.
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Using Aspen HYSYS Upstream for Sizing and Scheduling of Gathering Systems
1. Authors: Francisco da Silva, James Holoboff, Ahad Sarraf Shirazi (Process Ecology Inc.)
30 June, 2015
Using Aspen HYSYS® Upstream for Sizing
and Scheduling of Gathering Systems
James Holoboff, Managing Partner, Process Ecology Inc.