API th Edition Ballot Item 7.8 Work Item 4 Gas Breakthrough
|
|
- Maud Morris
- 5 years ago
- Views:
Transcription
1 API th Edition Ballot Item 7.8 Work Item 4 Gas Breakthrough NOTE: This is a reballot of previously approved API th Edition Ballot Item 6.3 which was modified based on comments. Comments should only address changes being balloted, truly address technical issues if they are technical comments, and propose alternative language. Background Work Item 4: # Source Section Comment Proposed Change Volunteer 4 6 th Edition Ballot 2 comme nt 67; ballot 3 comme nt API th Edition Ballot 2: Add new criteria on liquid displacement considerations following gas blowby. Ballot 3: Liquid displacement can occur due to number of scenarios that involve HP/LP interfaces (Reverse flow, tube rupture, etc) not just vapor breakthrough. I would like to suggest that this be a possibly be part of a separate section that looks at this subject on from a higher level and then provide detail for individual scenarios. Liquid displacement definition will be included. Solutions (mitigation plans) will be included, such as increasing the volume of downstream vessel, installing a relief device upstream. Cascading break through will not be included in the first draft API th Edition Ballot 2: If the vapour space is insufficient to prevent the downstream vessel from filling prior to gas breakthrough, pressure relief valves sized only for the gas breakthrough flow may not prevent overpressure of the vessel. Overpressure may be prevented by one of the following options sizing the pressure relief valves to discharge liquid at the volumetric equivalent of the incoming vapour flow increasing the size of the downstream vessel to provide additional vapour space to accommodate the maximum anticipated liquid inventory providing a HIPS on the high pressure vessel which isolates the flow to the low pressure vessel on low liquid level. Evaluate cascading break through. P. Frey; M. Brewer; M. Porter; E. Vatland Johansen; T. Bevilacqua; K. Campbell; L. Mcdaniel; W. Ciolek; J. Burgess; F. Self / A. Aldeeb
2 Proposed Modifications to API th Ed: 1. Add the following sentence at the end of Paragraph 3 in Section Annex G provides additional considerations to evaluate the impact of the vapor breakthrough or gas blowby on low-pressure system and overpressure relief requirements. 2. Add Annex G (Informative) Liquid Displacement : Annex G (Informative) Vapor Breakthrough into Liquid- containing SystemsDisplacement Failure of high-pressure vessel liquid bottoms level control and bypass valves discharging into a low-pressure system may result in significant increase in the lowpressure system liquid level. Depending on the high-pressure and low-pressure systems volumes and liquid inventories, the low-pressure downstream system may liquid overfill. Of special concern, in certain cases this scenario may be followed by loss of liquid level in the high-pressure system that can result in Vapor vapor breakthrough through the inlet level control and bypass valves to the low-pressure systems (the scenario described in Section ) is generally preceded by the high-pressure system vapor phase displacing the liquid phase in the low-pressure system until eventually vapor breakthrough occurs at the inlet control valve. As the vapor passes through the inlet level control valve, the vapor will expand and push (displace) the liquid in the downstream system until a relief path is established. This transient scenario is commonly described as liquid displacementthis is commonly described as liquid displacement. During the scenario, the liquid level in the low-pressure vessel can rise creating the potential for liquid or two-phase relief. This can result in increased lowpressure system relief requirements relative to a vapor breakthrough with only vapor relief. Due to the difficulties of establishing the required relieving capacity and ensuring that this is continuously available, it is conservatively assumed no credit is taken for
3 vapor outflow and the low-pressure system reaches relieving pressure. The consequences of liquid displacement are very sensitive to the size of the low-pressure system and liquid inventories in the high and low-pressure systems prior to the start of the scenario. Hence, a review should be undertaken to identify the worst case operating conditions for the liquid displacement assessment including consideration of non-routine situationsincluding process start-up and shutdown. In this annexsection, general considerations are described to identify potential liquid displacement relief requirements associated with the vapor breakthrough scenarios. Other publications provide more detailed guidanceinformation on liquid displacement analysis [1] [2]. It should also be noted that other overpressure scenarios may result in similar liquid displacement effect such as control valve failure, heat exchanger tube rupture, inadvertent opening of manual valves, reverse flow, instrument air failure, or power failure. However, these scenarios are not addressed in this section. The phase quality and flowrate of the relieved stream depends on following factors: high and low pressure systems operating temperature and pressure; high and low pressure systems fluid composition; high and low pressure systems liquid levels; i.e., liquid inventories; prior to failure of the inlet valve(s) liquid-vapor onset/disengagement regime: foamy, bubbly, and churn-turbulent fluids; vapor superficial velocity in low-pressuredownstream vessel; low-pressure vessel orientation (vertical or horizontal); low-pressure vessel and inlet nozzle elevation; low-pressure vessel inlet flow distributor geometry and orientation (if present); location of the pressure relief device; and assumption for continuation of high-pressure and low-pressure systems liquid outflows at normal minimum rates Depending on the high and low pressure systems liquid inventories, there are two potential relief scenarios that may be relevant: A. Upstream system liquid inventory is less than the downstream system vapor volume at relief conditions. The user should determine the liquid level in the low-pressure vessel assuming all of the liquid from the high-pressure vessel is transferred. A vapor-liquid disengagement analysis should then be performed to determine the phase of the
4 relief stream. The DIERS Project Manual [3] and the CCPS Guidelines for Pressure Relief and Effluent Handling Systems [4] provide guidance to determine if two phase relief will occur due to liquid swell (e.g., the increase in liquid level due to liquid and vapor mixing) or liquid entrainment caused by the velocity of the vapor across the surface of the liquid. Complete vapor-liquid disengagement with no liquid entrainment will result in vapor relief. The Required required vapor relief rate should be determined using the guidance provided in Section In case it is assumed that liquid will continue to flow from the high-pressure system, then the impact of flashing liquid on relief requirements should be evaluated. However, if the vapor-liquid disengagement analysis revealed reveals a two-phase flow, then the guidance provided in the DIERS Project Manual [3] and the CCPS Guidelines for Pressure Relief and Effluent Handling Systems [4] can be used to estimate the two-phase relief stream quality. This guidance considers the fluid regime, i.e., foamy, bubbly, or churn-turbulent. The required relief rate should be equal to the volumetric flow of fluid entering the system through flow limiting element (wide-open control valve, bypass valve, restriction orifice) at relief conditions taking into consideration the mixing with swelled liquid phasebased on the volumetric vapor flow rate through wide-open control and/or bypass valves mixed with the swelled liquid phase. If the low-pressure vessel s inlet nozzle becomes submerged, then when the vapor breakthrough occurs the vapor will be sparged into the low-pressure vessel causing the liquid level to rise further. If it is determined User should evaluate if a that twophase relief will not occur due to inadequate vapor-liquid disengagement, then two phase flow or due to high flow vapor re-entrainingentrainment of liquid should be considered[2]. B. Upstream system liquid inventory is more than the downstream system vapor volume at relief conditionsthe vapor volume in the downstream system is insufficient to prevent it from filling with liquid prior to vapor breakthrough. In this case, the low pressure vessel overfills before the vapor breakthrough occurs. The initial relief will be a steady-state liquid relief (or steady-state two-phase relief). However, it is expected that the liquid level in the high-pressure vessel will eventually be lost which would result in vapor breakthrough. Since the low-pressure system is full, The the required relief rate should be calculated based on the displaced liquid at a rate equal to the volumetric flow of fluid entering the system through the flow limiting element (wide-open control valve, bypass valve, restriction orifice) at relief
5 conditions volumetric rate equivalent to the actual volumetric vapor flow rate through the flow limiting element (wide-open control valve, bypass valve, restriction orifice). Liquid displacement should be calculated using liquid and vapor densities at the relieving conditions. The user may apply a credit for continuous high-pressure system liquid out flow to reduce the vapor breakthrough rate across the control valve and hence reduce the liquid displacement relief rate. In these cases, the vapor phase density in the lowpressure system should account for liquid flashing at relief conditions. It should be noted that the relief rate calculated for liquid displacement almost invariablyoften results in inadequate substantial relief requirements capacity due to substantially large liquid relief rate. The following options may be considered to mitigate the overpressure scenario or reduce the relief requirements of liquid displacement: Designing an inherently safer system by increasing the low-pressure system MAWP to eliminate the applicability of the overpressure scenario. However, the impact on the equipment downstream of the low-pressure system should be evaluated. Increasinge the size and vessel capacity of the low- pressure system to allow vapor-liquid disengagement to occur and to prevent overfillingincreasing the size of the low pressure system. Modifying the liquid levels to provide additional vapor space to accommodate the maximum anticipated liquid inventory. Providing HIPS on the high pressure system which isolates the flow to the low pressure system on low liquid level in the high pressure system and/or high level in the low pressure system. Providinge HIPS on the low-pressure system to progressively open a dump valve which would allow liquid to leave the low-pressure system and prevent low-pressure system. Performing detailed dynamic simulation of inlet control valve failure and potential liquid displacement per guidance in Section Sizing the pressure relief devices for liquid displacement. Restricting inlet flow through the flow limiting element. Taking credit for reduction in relieving flow due to flowing resistance in full segment piping between high-pressure and low-pressure systems. Considering downstream overfill protection per guidance in Section
6 Determininge if credit can be taken for the downstream system out flow paths. If the selected option to mitigate the overpressure scenario or reduce the relief requirements of liquid displacement resulted in liquid release to the disposal system, then the impact on PRD size, slug flow in disposal system piping, and knockout drum capacity should be evaluated. References: [1] N. Faulk and A. Aldeeb, Understanding Gas Blowby Scenario Calculations, Proceedings of the 11th Global Congress on Process Safety, American Institute of Chemical Engineers, Austin, Texas, 2015 [2] G. Melhem, M. Brewer, and M. Porter, The Anatomy of Liquid Displacement and Vapor Breakthrough, Proceedings of the 12th Global Congress on Process Safety, American Institute of Chemical Engineers, Houston, Texas, 2016the Spring 2014 DIERS Users Group Meeting, Houston, Texas [3] H. G. Fisher, et al., Emergency Relief System Design Using DIERS Technology, ISBN , American Institute of Chemical Engineers, New York, 1992 [4] CCPS, Guidelines for Pressure Relief and Effluent Handling Systems, 2017, ISBN
Steam generator tube rupture analysis using dynamic simulation
Steam generator tube rupture analysis using dynamic simulation Heat Exchangers are used to transfer heat from a hot fluid to a cold fluid. Most of the times these fluids are available at different pressures
More informationChanges Between API STD 521 6th Ed and 5th Ed Cataloged
Changes Between API STD 521 6th Ed and 5th Ed Cataloged Dustin Smith Smith & Burgess LLC 7600 W Tidwell, Houston, TX Dustin.Smith@smithburgess.com John Burgess Jarrett Doe Smith & Burgess LLC 7600 W Tidwell,
More informationChallenges in Relief Design for Pilot Plants
Challenges in Relief Design for Pilot Plants Published on July 5, 2017 Michael Trainor Relief system design at the pilot scale presents unique challenges that don t always apply at the commercial scale.
More informationPRESSURE RELIEF VENTING SYSTEMS EXAMPLES OF GOOD AND BAD PRACTICE
PRESSURE RELIEF VENTING SYSTEMS EXAMPLES OF GOOD AND BAD PRACTICE John Hare and Michael Johnson, Health and Safety Laboratory, Buxton, UK Pressure relief systems employed at chemical and petrochemical
More information44 (0) E:
FluidFlow Relief Valve Sizing Handbook Flite Software 2016 Flite Software N.I. Ltd, Block E, Balliniska Business Park, Springtown Rd, Derry, BT48 0LY, N. Ireland. T: 44 (0) 2871 279227 E: sales@fluidflowinfo.com
More informationChanges Between API STD 520 Part II 6th Ed and 5th Ed Cataloged
Changes Between API STD 520 Part II 6th Ed and 5th Ed Cataloged Dustin Smith Smith & Burgess LLC 7600 W Tidwell, Houston, TX Dustin.Smith@smithburgess.com John Burgess Jessye Palladino Smith & Burgess
More informationTransient Analyses In Relief Systems
Transient Analyses In Relief Systems Dirk Deboer, Brady Haneman and Quoc-Khanh Tran Kaiser Engineers Pty Ltd ABSTRACT Analyses of pressure relief systems are concerned with transient process disturbances
More informationTube rupture in a natural gas heater
Tube rupture in a natural gas heater Dynamic simulation supports the use of a pressure safety valve over a rupture disk in the event of a tube rupture HARRY Z HA and PATRICK STANG Fluor Canada Ltd A fast
More informationScaling Up Safely: Making Smarter Decisions about Rate Dependency
Scaling Up Safely: Making Smarter Decisions about Rate Dependency Zubin Kumana, P.E., Venkata Badam,P.E., and Achilles Arnaez, P.E. 7600 W. Tidwell Rd., Ste. 600 Houston, TX 770400 (713) 802-2647 SmithBurgess.com
More informationTutorial. BOSfluids. Relief valve
Tutorial Relief valve The Relief valve tutorial describes the theory and modeling process of a pressure relief valve or safety valve. It covers the algorithm BOSfluids uses to model the valve and a worked
More informationBROCHURE. Pressure relief A proven approach
BROCHURE Pressure relief A proven approach 2 PRESSURE RELIEF A PROVEN APPROACH Pressure relief Pressure relief systems are a vital layer of protection for your processes. To provide this protection, systems
More informationHANDBOOK SAFETY DEVICES. Ed SAFETY DEVICES DS-ED 01/ ENG 1
HANDBOOK Ed. 2017 1 CHAPTER 5 SELECTION CRITERIA FOR SAFETY VALVES CALCULATION OF THE DISCHARGE CAPACITY (Ref. EN 13136:2013) The evaluation of the minimum required discharge capacity of safety valves
More informationINHERENTLY SAFER DESIGN CASE STUDY OF RAPID BLOW DOWN ON OFFSHORE PLATFORM
INHERENTLY SAFER DESIGN CASE STUDY OF RAPID BLOW DOWN ON OFFSHORE PLATFORM Volton Edwards bptt Angus Lyon DNV Energy Alastair Bird DNV Energy INTRODUCTION A term now in common usage within the oil & gas
More informationVENDOR SUPPLIED EQUIPMENT: ENSURING PSV DESIGN MEETS PSV SPEC
VENDOR SUPPLIED EQUIPMENT: ENSURING PSV DESIGN MEETS PSV SPEC Jeffrey Heil, P.E. Inglenook Engineering, Inc. 15306 Amesbury Lane Sugarland, TX 77478 jeff@inglenookeng.com 832-457-1862 Brian Pack, P.E.*
More informationSafety Selector Valves Dual Pressure Relief Device System
ANDERSON GREENWOOD Features and enefits Provides a safe, efficient method of switching from an active pressure relief device to a standby, maintaining system overpressure protection regardless of Safety
More informationCOMPONENT AVAILABILITY EFFECTS FOR PRESSURE RELIEF VALVES USED AT HYDROGEN FUELING STATIONS
COMPONENT AVAILABILITY EFFECTS FOR PRESSURE RELIEF VALVES USED AT HYDROGEN FUELING STATIONS Moussin Daboya-Toure, M.D-T. 1, Robert Burgess, R.B. 2 and Aaron Harris, A.H. 3 1 Air Liquide Advanced Technologies,
More informationWHITE PAPER. SmartPlant P&ID Engineering Integrity 10 Example Rules
WHITE PAPER SmartPlant P&ID Engineering Integrity 10 Example Rules SmartPlant P&ID Engineering Integrity SmartPlant P&ID Engineering Integrity checks that SmartPlant P&IDs comply with engineering standards
More informationCOMMITTEE DRAFT. API 520 Part I 10 th Edition Ballot Item 2.1. This ballot covers the following item:
This ballot covers the following item: API 520 Part I 10 th Edition Ballot Item 2.1 2008 12 Modify guidance to PRV datasheets (Line 17) to assist user s with determining the temperature to use for selecting
More informationQuantitative Risk Analysis (QRA)
Quantitative Risk Analysis (QRA) A realistic approach to relief header and flare system design Siemens AG 2017, All rights reserved 1 Quantitative Risk Analysis Introduction Most existing pressure relief
More informationLooking Beyond Relief System Design Standards
Looking Beyond Relief System Design Standards M. Reilly & T. Craddock Introduction A correctly designed relief system is key to safe plant design and operation, ensuring the ability to handle any potential
More informationFrequently Asked Questions Directive 056 Facilities Technical
Frequently Asked Questions Directive 056 Facilities Technical October 2017 This document clarifies and supports some of the technical requirements related to Directive 056: Energy Development Applications
More information6.6 Relief Devices. Introduction
6.6 Relief Devices Introduction Relief devices are used to help prevent a catastrophic failure of equipment and/or minimize the effects of any unanticipated or uncontrolled events. As such, relief devices
More informationSELECTION CRITERIA FOR SAFETY VALVE
mdmdmdpag 1 di 17 SELECTION CRITERIA FOR SAFETY VALVE CALCULATION OF THE DISCHARGE CAPACITY (Ref. EN 13136:2013) The calculation of the minimum discharge capacity is linked to the system configuration
More informationJournal of Applied Fluid Transients, Vol 1-1, April 2014 (3-1)
Modeling and Field Verification Study of Air Slam Conditions on kalanit Pipeline System By Yiftach Brunner & Sathish Kumar ir valves are integral part of long water transmission mains and are essential
More informationOperational Settings:
instrucalc features more than 70 routines associated with control valves, ISO flow elements, relief valves and rupture disks, and calculates process data at flow conditions for a comprehensive range of
More informationThe capacity of the cargo tank venting system (46 CFR );
INDUSTRY GUIDELINES FOR DETERMINING THE MAXIMUM LIQUID TRANSFER RATE FOR A TANK VESSEL TRANSFERRING A FLAMMABLE OR COMBUSTIBLE CARGO USING A VAPOR CONTROL SYSTEM This document provides guidance from the
More informationA Study of Pressure Safety Valve Response Times under Transient Overpressures
A Study of Pressure Safety Valve Response Times under Transient Overpressures B C R Ewan, Chemical & Biological Engineering Department, University of Sheffield, Mappin St, Sheffield, S1 3JD. C Weil, 7
More informationEvery things under control High-Integrity Pressure Protection System (HIPPS)
Every things under control www.adico.co info@adico.co Table Of Contents 1. Introduction... 2 2. Standards... 3 3. HIPPS vs Emergency Shut Down... 4 4. Safety Requirement Specification... 4 5. Device Integrity
More informationRadar, Ultrasonic and RF Level Transmitters
Radar, Ultrasonic and RF Level Transmitters Both measures the time it takes the wave to travel between the transmitter and that reflected wave off the surface of the material to reach the transmitter again.
More informationPressure Relief Valve Inspection Interval
Pressure Relief Valve Inspection Interval Thiago Trotta, Charles Kashou, and Nancy Faulk Siemens Energy, Inc, 4615 Southwest Fwy, Suite 900, Houston, TX 77027; nancy.faulk@siemens.com (for correspondence)
More informationNORMAL OPERATING PROCEDURES Operating Parameter Information
Operating Parameter Information Each operator performing the normal operating procedures (routine checks) of the facility should be familiar with the current normal operating parameters of all systems
More informationPigging as a Flow Assurance Solution Avoiding Slug Catcher Overflow
Pigging as a Flow Assurance Solution Avoiding Slug Catcher Overflow Aidan O'Donoghue, Pipeline Research Limited, Glasgow, UK This paper sets out to provide an initial method of assessing the bypass requirements
More informationThis portion of the piping tutorial covers control valve sizing, control valves, and the use of nodes.
Piping Tutorial A piping network represents the flow of fluids through several pieces of equipment. If sufficient variables (flow rate and pressure) are specified on the piping network, CHEMCAD calculates
More informationThe Relationship Between Automation Complexity and Operator Error
The Relationship Between Automation Complexity and Operator Error presented by Russell Ogle, Ph.D., P.E., CSP rogle@exponent.com (630) 274-3215 Chemical Plant Control Control physical and chemical processes
More informationSmart Water Application Technologies (SWAT) TM
Smart Water Application Technologies (SWAT) TM Equipment Functionality Test Protocol Version 2.3 June 2014 SWAT Committee 8280 Willow Oaks Corporate Drive Suite 400 Fairfax, VA 22031 www.irrigation.org
More informationInjector Dynamics Assumptions and their Impact on Predicting Cavitation and Performance
Injector Dynamics Assumptions and their Impact on Predicting Cavitation and Performance Frank Husmeier, Cummins Fuel Systems Presented by Laz Foley, ANSYS Outline Overview Computational Domain and Boundary
More informationSizing, Selection, and Installation of Pressure-relieving Devices in Refineries
Sizing, Selection, and Installation of Pressure-relieving Devices in Refineries Part I Sizing and Selection Downstream Segment API STANDARD 520 EIGHTH EDITION, DECEMBER 2008 Special Notes API publications
More informationRelief System Sizing for Runaway Chemical Reactions: A Simple Comprehensive Approach
Relief System Sizing for Runaway Chemical Reactions: A Simple Comprehensive Approach Ken Kurko Fauske & Associates, LLC 16W070 83 rd Street Burr Ridge, IL 60527 kurko@fauske.com Prepared for Presentation
More informationImproving Accuracy of Frequency Estimation of Major Vapor Cloud Explosions for Evaluating Control Room Location through Quantitative Risk Assessment
Improving Accuracy of Frequency Estimation of Major Vapor Cloud Explosions for Evaluating Control Room Location through Quantitative Risk Assessment Naser Badri 1, Farshad Nourai 2 and Davod Rashtchian
More informationBefore You Fix the Relief Valve Problem
Before You Fix the Relief Valve Problem Careful considerations when mitigating inadequate relief systems designs Jason Spearow, P.E Presenter Biography Jason Spearow, P.E. Smith & Burgess LLC Senior Process
More informationValve Sizing Considerations. Steven Hocurscak Metso Automation
Valve Sizing Considerations Steven Hocurscak Metso Automation Oversizing Your Valves Issue with oversized valve A valve that is oversized can cause premature failure of valve trim or body - Oversized valves
More informationSAFETY SEMINAR Rio de Janeiro, Brazil - August 3-7, Authors: Francisco Carlos da Costa Barros Edson Romano Marins
SAFETY SEINAR Rio de Janeiro, Brazil - August 3-7, 2009 Using HAZOP and LOPA ethodologies to Improve Safety in the Coke Drums Cycles Authors: Gilsa Pacheco onteiro Francisco Carlos da Costa Barros Edson
More informationAPI th Edition Ballot Item 6.8 Work Item 54 Global Air Failure
API 521 7 th Edition Ballot Item 6.8 Work Item 54 Global Air Failure Background Work Item 54: # Source Section Comment Proposed Change Volunteer 54 Fall 2014 meeting Global instrument air failure scenario
More informationWhat is pressure relief valve? Pressure relief valve
What is pressure relief valve? Pressure relief valve What is: Relief valve Safety valve Safety relief valve Type of pressure relief valve Pressure relief valve sizing base What are the sizing basis of
More informationAir Eliminators and Combination Air Eliminators Strainers
Description Air Eliminators and Combination Air Eliminator Strainers are designed to provide separation, elimination and prevention of air in piping systems for a variety of installations and conditions.
More informationCPE562 Chemical Process Control HOMEWORK #1 PROCESS & INSTRUMENTATION DIAGRAM
Faculty of Chemical Engineering CPE562 Chemical Process Control HOMEWORK #1 PROCESS & INSTRUMENTATION DIAGRAM SUBMISSION DATE: 1 OCT. 2012 Question 1 Name the following equipments based on standard P&ID
More informationCHE Well Testing Package/Service:
CHE Well Testing Package/Service: CHE delivers well testing package And services, trailer mounted well testing package and offshore/onshore well testing services with over 10 years experience. Our testing
More informationOLGA. The Dynamic Three Phase Flow Simulator. Input. Output. Mass transfer Momentum transfer Energy transfer. 9 Conservation equations
서유택 Flow Assurance The Dynamic Three Phase Flow Simulator 9 Conservation equations Mass (5) Momentum (3) Energy (1) Mass transfer Momentum transfer Energy transfer Input Boundary and initial conditions
More informationENSURING AN ACCURATE RESULT IN AN ANALYTICAL INSTRUMENTATION SYSTEM PART 1: UNDERSTANDING AND MEASURING TIME DELAY
ENSURING AN ACCURATE RESULT IN AN ANALYTICAL INSTRUMENTATION SYSTEM PART 1: UNDERSTANDING AND MEASURING TIME DELAY Process measurements are instantaneous, but analyzer responses never are. From the tap
More informationJOSOP 603 flaring and venting Standard
JOSOP 603 flaring and venting Standard Dec, 2010 Approved December 29, 2010 Version 01 Posted February 3, 2011 Table of Contents 1.0 Purpose, Objectives and Scope... 3 1.1 Purpose... 3 1.2 Objective...
More informationSEPARATION SYSTEMS. The Separation Systems consists of the Test Header (GAY-0302) and the Test Separator (MBD-4501).
SEPARATION SYSTEMS The Separation Systems consists of the Test Header (GAY-0302) and the Test Separator (MBD-4501). The Header System is designed to collect and direct the well stream to the corresponding
More informationPressure Relief Valves is there a need when there are EDVs?
Pressure Relief Valves is there a need when there are DVs? Glenn Pettitt, nvironmental Resources Management, xchequer Court, 33 St Mary Axe, London, C3A 8AA Philip Pennicott, agip kco, Frontier Plaza,
More informationThe API states the following about tube rupture for a shell-and-tube heat exchangers:
Tutorial This tutorial describes the theory and modeling process of a tube rupture event using the special element type Rupture element in BOSfluids. It covers the algorithm BOSfluids uses to model the
More informationDesigning to proposed API WHB tube failure document
Designing to proposed API WHB tube failure document Dennis H. Martens Consultant and Technical Advisor (martensdh@pm-engr.com) Porter McGuffie Inc. Lon Stern Consultant (lhstern@earthlink.net) Stern Treating
More informationOIL SUPPLY SYSTEMS ABOVE 45kW OUTPUT 4.1 Oil Supply
OIL SUPPLY SYSTEMS ABOVE 45kW OUTPUT 4.1 Oil Supply 4.1.1 General The primary function of a system for handling fuel oil is to transfer oil from the storage tank to the oil burner at specified conditions
More informationFree Surface Flow Simulation with ACUSIM in the Water Industry
Free Surface Flow Simulation with ACUSIM in the Water Industry Tuan Ta Research Scientist, Innovation, Thames Water Kempton Water Treatment Works, Innovation, Feltham Hill Road, Hanworth, TW13 6XH, UK.
More informationTirpur Area Water Supply Project A Report on Transient Modeling Study
y February 2008 1 of 81 y INTRODUCTION: The report presents results from a transient modeling study conducted on the clear water transmission main of Tirpur Areas Water Supply Project, Tamilnadu, India.
More informationOIL AND GAS SEPARATION DESIGN MANUAL
OIL AND GAS SEPARATION DESIGN MANUAL BY C. RICHARD SIVALLS, P.E. SIVALLS, INC. BOX 2792 ODESSA, TEXAS 79760 All rights reserved. This publication is fully protected by copyright and nothing that appears
More informationA large Layer of Protection Analysis for a Gas terminal scenarios/ cause consequence pairs
A large Layer of Protection Analysis for a Gas terminal 2000+ scenarios/ cause consequence pairs Richard Gowland European process Safety Centre The scope of the study was a large gas terminal handling
More informationLARGE-SCALE EVALUATION OF VENT-SIZING METHODOLOGY FOR VAPOUR-PRESSURE SYSTEMS
LARGE-SCALE EVALUATION OF VENT-SIZING METHODOLOGY FOR VAPOUR-PRESSURE SYSTEMS T J Snee 1,2, J Bosch Pagans 1, L Cusco 1, F Gallice 1,3, C Hoff 1,3, D C Kerr 1, A Rovetta 1,3 and M Royle 1 1 Health and
More informationPractical Guide. By Steven T. Taylor, P.E., Member ASHRAE
ractical Guide The following article was published in ASHRAE Journal, March 2003. Copyright 2003 American Society of Heating, Refrigerating and Air- Conditioning Engineers, Inc. It is presented for educational
More informationYutaek Seo. Subsea Engineering
Yutaek Seo Subsea Engineering Inlet receiving Gas and liquids that enter the gas processing facilities pass emergency shutdown valves, and then go to inlet receiving, where condensed phases drop out. Gas
More informationModelling of the Separated Geothermal Water Flow between Te Mihi flash plants
Proceedings World Geothermal Congress 2015 Melbourne, Australia, 19-25 April 2015 Modelling of the Separated Geothermal Water Flow between Te Mihi flash plants Kevin Koorey, Kim Harwood and Norman Lawgun
More informationSuppress Your Surges: Surge Suppression Fundamentals. April 13, 2017
Suppress Your Surges: Surge Suppression Fundamentals April 13, 2017 How Bad Can Waterhammer Really Be? 2 Workshop Agenda What is waterhammer? Causes of waterhammer Instantaneous surge pressures Surges
More informationDigester Processes. 1. Raw Sludge Pumping System
Digester Processes 1. Raw Sludge Pumping System Removes accumulated sludge from the primary clarifiers, pumped through 1 of 2 pipes either 150 or 200mm in diameter (Fig. 1.1). Fig 1.1 Pipes feeding Digesters
More informationHomework #14, due Wednesday, Nov. 28 before class. Quiz #14, Wednesday November 28 at the beginning of class
ANNOUNCEMENTS Homework #14, due Wednesday, Nov. 28 before class Conceptual questions: Chapter 14, #8 and #16 Problems: Chapter 14, #58, #66 Study Chapter 14 by Wednesday Quiz #14, Wednesday November 28
More informationLAKOS Waterworks. PWC Series Sand Separators. Installation & Operation Manual LS-829 (10/12)
LAKOS Waterworks PWC Series Sand Separators Installation & Operation Manual LS-829 (10/12) Table of Contents Separator Operation... 3 Individual Model Details.... 4 Flow vs. Pressure Loss Chart 4 Installation
More informationCANDU ORIGINS AND EVOLUTION PART 5 OF 5. THE ORIGINS & EVOLUTION OF THE SECOND SHUTDOWN SYSTEM by G.L. Brooks February
CANDU Origins and Evolution Part 5 of 5 1 CANDU ORIGINS AND EVOLUTION PART 5 OF 5 THE ORIGINS & EVOLUTION OF THE SECOND SHUTDOWN SYSTEM by G.L. Brooks 1-2001 February Prepared as a contribution to a project
More informationPETROLEUM & GAS PROCESSING TECHNOLOGY (PTT 365) SEPARATION OF PRODUCED FLUID
PETROLEUM & GAS PROCESSING TECHNOLOGY (PTT 365) SEPARATION OF PRODUCED FLUID Miss Nur Izzati Bte Iberahim Introduction Well effluents flowing from producing wells come out in two phases: vapor and liquid
More informationHazard Operability Analysis
Hazard Operability Analysis Politecnico di Milano Dipartimento di Energia HAZOP Qualitative Deductive (search for causes) Inductive (consequence analysis) AIM: Identification of possible process anomalies
More informationAPI Standard Venting Atmospheric and Low-Pressure Storage Tanks: Nonrefrigerated and Refrigerated
General API Standard 2000 - Venting Atmospheric and Low-Pressure Storage Tanks: Is there any limit for the maximum allowable linear velocity or any other parameter for the roof of a floating roof tank
More informationTABLE OF CONTENT
Page : 1 of 11 Project Engineering Standard www.klmtechgroup.com KLM Technology #03-12 Block Aronia, Jalan Sri Perkasa 2 Taman Tampoi Utama 81200 Johor Bahru Malaysia TABLE OF CONTENT SCOPE 2 REFERENCES
More informationHow to Optimize the Disposal System With Staggered Analysis Using BLOWDOWN Technology. Jump Start Guide
How to Optimize the Disposal System With Staggered Analysis Using BLOWDOWN Technology Jump Start Guide Problem Statement In this guide, you will be introduced to the tools in BLOWDOWN that can be used
More informationTemperature Controllers
IM0004 April 2013 CONTENTS T-12 Thermostat PAGE Introduction 1 Scope 1 Description 1 Specification 1 Temperature Controllers 2 INTRODUCTION CAUTION Prior to installing, the instructions provided herein
More informationIdentification and Screening of Scenarios for LOPA. Ken First Dow Chemical Company Midland, MI
Identification and Screening of Scenarios for LOPA Ken First Dow Chemical Company Midland, MI 1 Layers of Protection Analysis (LOPA) LOPA is a semi-quantitative tool for analyzing and assessing risk. The
More informationWorkshop 302-compressor-anti-surge
Workshop Objectives Workshop 302-compressor-anti-surge Illustrate how to create a simple anti-surge control on a compressor Workshop Description Flowsheeet: A feed stream at 1 bar with methane, ethane
More informationHANDBOOK SAFETY DEVICES. Ed SAFETY DEVICES DS-ED 01/ ENG 1
HANDBOOK Ed. 2017 DS-ED 01/2017 - ENG 1 CHAPTER 9 BURSTING DISC DEVICES IN SERIES 3070 SCOPE Use: protection against possible overpressure of the apparatuses listed below, with regard to the operating
More informationDynamic Simulation for T-9 Storage Tank (Holding Case)
Dynamic Simulation for T-9 Storage Tank (Holding Case) CASE 1: 19,642 Kg/Hr (Holding: 52 o C), No Liquid Draw Workshop Description Estimation of vapor flow rate coming out from the T-9 tank for holding
More informationDYNAMIC BEHAVIOR OF SPRING-LOADED PRESSURE RELIEF VALVE: NUMERICAL AND EXPERIMENTAL ANALYSIS
Proceedings of the 2012 9th International Pipeline Conference IPC2012 September 24-28, 2012, Calgary, Alberta, Canada IPC2012-90239 DYNAMIC BEHAVIOR OF SPRING-LOADED PRESSURE RELIEF VALVE: NUMERICAL AND
More informationFloat Operated Level Controllers
CONTENTS Float Operated Level Controllers IM0015 Nov. 2014 PAGE Introduction 1 Scope 1 Description 1 Specification 1 Control Installation 2 INTRODUCTION Side Mount Back Mount Prior to installing, the instructions
More informationUsing LOPA for Other Applications
10 Using LOPA for Other Applications 10.1. Purpose LOPA is a tool used to perform risk assessments. Previous chapters described its use in assessing the risk level of process hazards scenarios and in evaluating
More informationRELIEF VALVES IN PARALLEL
RELIEF VALVES IN PARALLEL Mary Kay O'Connor Process Safety Center International Symposium BEYOND REGULATORY COMPLIANCE MAKING SAFETY SECOND NATURE October 26-28, 2010 James R. Lawrence Sr. Why use a Relief
More informationProcess Safety and the Human Factor
Process Safety and the Human Factor INTRODUCTION The increasing lifetime of industrial processing plants creates a growing challenge for plant owners/operators to continue to run in a safe and efficient
More informationThe Discussion of this exercise covers the following points: Pumps Basic operation of a liquid pump Types of liquid pumps The centrifugal pump.
Exercise 2-3 Centrifugal Pumps EXERCISE OBJECTIVE In this exercise, you will become familiar with the operation of a centrifugal pump and read its performance chart. You will also observe the effect that
More informationFisher DVI Desuperheater Venturi Inline
Instruction Manual DVI Desuperheater Fisher DVI Desuperheater Venturi Inline Contents Introduction... 1 Scope of Manual... 1 Description... 1 Principle of Operation... 2 Installation... 3 Operating Instructions...
More informationProposed Abstract for the 2011 Texas A&M Instrumentation Symposium for the Process Industries
Proposed Abstract for the 2011 Texas A&M Instrumentation Symposium for the Process Industries Focus Area: Automation HMI Title: Author: Shared Field Instruments in SIS: Incidents Caused by Poor Design
More informationA review of best practices for Selection, Installation, Operation and Maintenance of Gas meters for Flare Applications used for Managing facility
A review of best practices for Selection, Installation, Operation and Maintenance of Gas meters for Flare Applications used for Managing facility mass balance and compliance 1. What, When and Why? 2. Flare
More informationCommittee on NFPA 85
Committee on NFPA 85 M E M O R A N D U M TO: FROM: NFPA Technical Committee on Heat Recovery Steam Generators Jeanne Moreau DATE: April 23, 2010 SUBJECT: NFPA 85 F10 ROC Letter Ballot The ROC letter ballot
More informationThe Discussion of this exercise covers the following points:
Exercise 3-2 Orifice Plates EXERCISE OBJECTIVE In this exercise, you will study how differential pressure flowmeters operate. You will describe the relationship between the flow rate and the pressure drop
More informationIRC 2011 All Rights Reserved
1 2 3 The enthalpy of saturated vapor and the enthalpy of saturated liquid is evaluated at the fully accumulated relief device set pressure (P=P set * 1.1 + 14.7). Set Pressure (psig) h fg (Btu/lbm) 150
More informationGas Lift Valve Testing
36 th Gas-Lift Workshop Stavanger, Norway February 4 8, 2013 Gas Lift Valve Testing Angel Wileman, Research Engineer Southwest Research Institute, Fluid Dynamics Feb. 4 8, 2013 2013 Gas-Lift Workshop 1
More informationEASTERN ENERGY SERVICES PTE LTD. 60 Kaki Bukit Place #02-19 Eunos Tech Park Singapore, SG Singapore Telephone: Fax:
2 Table Of Contents 1. Introduction 3 2. About this Manual 3 3. Contacting YZ Systems 3 4. Vessel Components 4 5. Specifications 5 6. Application 6 7. Theory of Operation 7 8. DuraSite Installation & Use
More informationRestriction Orifice. Single or Multi Stage Orifice to. Reduce Pressure or. Limit the Flow Rate
Restriction Orifice Single or Multi Stage Orifice to Reduce Pressure or Limit the Flow Rate Restriction Orifice Plates Series ROPS Principle Restriction Orifice Plates and Critical Flow Devices and their
More informationGas Vapor Injection on Refrigerant Cycle Using Piston Technology
Purdue University Purdue e-pubs International Refrigeration and Air Conditioning Conference School of Mechanical Engineering 2012 Gas Vapor Injection on Refrigerant Cycle Using Piston Technology Sophie
More informationModeling a Pressure Safety Valve
Modeling a Pressure Safety Valve Pressure Safety Valves (PSV), Pressure Relief Valves (PRV), and other pressure relieving devices offer protection against overpressure in many types of hydraulic systems.
More informationNational Fire Protection Association. 1 Batterymarch Park, Quincy, MA Phone: Fax:
National Fire Protection Association 1 Batterymarch Park, Quincy, MA 02169-7471 Phone: 617-770-3000 Fax: 617-770-0700 www.nfpa.org M E M O R A N D U M TO: FROM: NFPA Technical Committee on Electrical Equipment
More informationGUIDANCE IN-SERVICE INSPECTION PROCEDURES
GUIDANCE IN-SERVICE INSPECTION PROCEDURES Number: PEC 13 Prepared by: Pressure Equipment Committee (TC1) Status: Issue: 07 Date: 16 th January 2018 Reference: Guidance for safety valve examination. SITUATION:
More informationFaculty of Science and Technology MASTER S THESIS. Writer: Rune Kvammen
Faculty of Science and Technology MASTER S THESIS Study program/ Specialization: Petroleum Engineering / Production technology Spring semester, 2011 Open access Writer: (Writer s signature) Faculty supervisor:
More informationDimensioning of Safety Valves Auditorium Tecnimont
Dimensioning of Safety Valves Auditorium Tecnimont 21.09.2016 Objective of the presentation Design of Safety Valves ASME VIII / API 520 The objective of the presentation is to show the design of safety
More informationImpact on People. A minor injury with no permanent health damage
Practical Experience of applying Layer of Protection Analysis For Safety Instrumented Systems (SIS) to comply with IEC 61511. Richard Gowland. Director European Process Safety Centre. (Rtgowland@aol.com,
More information