DYNAMIC SIMULATION FOR DESIGN IMPROVEMENTS, COST REDUCTION AND OPERATIONAL STABILITY IN LNG PLANT DESIGN
|
|
- Lewis Griffith
- 6 years ago
- Views:
Transcription
1 DYNAMIC SIMULATION FOR DESIGN IMPROVEMENTS, COST REDUCTION AND OPERATIONAL STABILITY IN LNG PLANT DESIGN SIMULATION DYNAMIQUE POUR L AMELIORATION DU PROCEDE, REDUCTION DES COUT, ET STABILITE DE L OPERATION D UN PROCEDE D UNE INSTALLATION DE GNL Satish L. Gandhi, Ph.D. Director - Process (LNG) Felix F. de la Vega, M.S. Vice President - Petroleum (LNG) Fluor Daniel, Inc. Sugarland, Texas, , U.S.A. ABSTRACT This paper discusses some of the dynamic and steady state simulation studies performed for LNG plants utilizing the APCI propane (C3) precooled mixed refrigerant () cycle which have resulted in or indicated the way towards design improvements and reduction in plant costs while ensuring stable operation. The dynamic studies presented include (a) reduction in flare header size and cost by minimizing the potential for release from refrigeration compressors; major failure scenarios considered are total and partial loss of power to C3 compressor s air-cooled exchanger fans, inadvertent closure of block valve at the outlet of C3 compressor, and inadvertent closure of block valve at the outlet of C3 receiver, and (b) elimination of pressure surge dampening equipment in LNG loading lines. The steady state design studies presented include (a) optimization of C3 condenser size for the specified availability of gas turbine power, and (b) sensitivity of LNG production to variations in compressor performance characteristics. RESUME Ce papier présente quelques études de simulation en régime dynamique et permanent du procédé APCI à cycle aux réfrigérants mélangés pré-refroidi résultant en ou menant dans une voie d une amélioration du procédé avec une réduction des coûts de l installation tout en assurant la stabilité de l opération. D.3 1
2 Les études présentées incluent; (a): une réduction de dimension du collecteur de torche ainsi que le coût en minimisant les fuites potentielles du compresseur de réfrigération, en considérant les scénarios de failles majeurs telles que: perte totale ou partielle de l énergie motrice du ventilateur de l échanger à air du compresseur de propane, fermeture inattentive de la vanne de sectionnement du refoulement du compresseur propane, et fermeture inattentive de la vanne de section de la ligne de soustirage du ballon accumulateur de propane, et (b): l élimination de l équipement d élimination de surpression dans les lignes de chargement de GNL. Les études de calcul en régime permanent présentées incluent, (a): optimization de la dimension du condenseur de propane pendant la disponibilité de l énergie motrice de la turbine à gaz, et (b) l analyse de sensibilité de la réponse du compresseur de réfrigération aux variations des caractéristiques de la performance du compresseur. INTRODUCTION This paper presents several studies performed for LNG plants which have resulted in or indicated the way towards design improvements and reduction in plant costs while at the same time ensuring stable operation. Most of these studies have been carried out utilizing an integrated dynamic process simulation model of the APCI propane precooled cycle in LNG plants. Since it is an integrated model, the effects of interactions between the C3 and refrigeration-compression systems are considered which is essential for addressing LNG plant dynamics and design issues. A schematic drawing of an APCI propane precooled cycle in an LNG plant with air cooling is shown in Figure 1. The dynamic process simulation model is built from a library of customized unit operation models of individual equipment and control systems specifically developed for LNG plant design. The dynamic simulation model converts into a steady state modeling tool by simply setting the time derivatives of state variables to zero. The model allows analysis of a wide range of problems related to the process design of LNG plant, either dynamic (time dependent) or steady state. The design issues addressed in this paper include the following: Flare header sizing and cost reduction Hydraulic surge analysis of the LNG loading system Optimum design of the C3 condenser Sensitivity of LNG production to variations in compressor performance curves FLARE HEADER SIZING AND COST REDUCTION The relief flows associated with major plant upsets are usually derived from steady state analysis. Such analyses ignore the dynamic interactions between various parts of the process. This approach also precludes a way to assess the impact of process or control system modifications that could be implemented for mitigating the maximum relief D.3 2
3 flows. These limitations lead to designing relief and flare header systems that are significantly oversized and costly. The dynamic process simulation model of the LNG plant developed at Fluor Daniel allows us to evaluate the actual dynamic response of the system to any potential failure or upset scenario within the LNG plant. The model also provides an efficient tool for evaluating design alternatives, such as high integrity instrumentation systems, for mitigating or eliminating the impact of plant failures. Three major plant upset scenarios usually considered for sizing the relief and flare header systems during the process design of an LNG project (assumed to be an air-cooled plant) are discussed below. FIGURE 1 LNG EXPANDER G M FLASH GAS COMPRESSOR TO FUEL GAS MERCURY DEHYDRATION REMOVAL UNIT UNIT HHP HP MP LP G EXPANDER LNG RUNDOWN TO STORAGE MAIN CRYOGENIC HEAT EXCHANGER GT M SYSTEM TO/FROM FRACTIONATION UNIT RECEIVER F LP MP HP HHP PROPANE SYSTEM GT M PROPANE RECEIVER LP MP HP HHP Loss of Power to C3 Compressor s Air-Cooled Exchanger Fans The dynamic response of the relief system to the total loss of power to the C3 compressor s air-cooled exchanger fan motors is shown in Figures 2 and 3. Even with the total loss of power, about 1% of air flow is maintained to account for natural convection. The flow and the back pressure at the relief valve are shown as % of the maximum allowable relief rate and back pressure requirements. The back pressure limitation at the relief valve is based on the lowest set pressure of the critical relief valves in the flare header system. The dynamic response of the relief rate at the flare tip is somewhat damped and delayed as compared to that at the relief valve due to the effect of packing in the flare header piping. The dynamic response shows that the total loss of power to the exchanger air fans would result in maximum relief rate and back pressure at the relief valve about 25% higher than the maximum allowable values. This would require increasing the pipe diameters for both the relief valve outlet header piping as well as the long main flare header piping to the flare stack resulting in a significant increase in the cost of the flare header system. D.3 3
4 An alternative for reducing the maximum relief flow is providing emergency power to some of the air fan motors in case of total loss of power. A dynamic simulation analysis was performed to evaluate the sensitivity of the relief rate and back pressure to the availability of emergency power. The results for 75% loss of power (or availability of emergency power to 25% of air fan motors) are shown in Figures 4 and 5 and for 5% loss of power (or availability of emergency power to 5% of air fan motors) are shown in Figures 6 and 7. It is seen that the relief flows as well as the back pressures at the relief valves are only about 5% and 25% of the maximum allowable value for the 75% and 5% loss of power, respectively. The analysis confirmed that providing emergency power to 25% of the air fans instead of increasing the size of the flare header piping is a cost effective solution to the total loss of power scenario. flow - % max Total Loss of Power flare tip relief valve rv back pressure - % max Total Loss of Power Figure 2 Figure 3 flow - % max 2 75% Loss of Power flare tip relief valve rv back pressure - % max 2 75% Loss of Power Figure 4 Figure 5 D.3 4
5 flow - % max 2 5% Loss of Power flare tip relief valve rv back pressure - % max 2 5% Loss of Power Figure 6 Figure 7 Inadvertent Closure of Block Valve at the Outlet of C3 Compressor with Bypass Relief Valve Similar to the loss of power scenario discussed earlier, dynamic simulation analysis of the inadvertent closure of the block valve in the discharge line of the C3 compressor showed maximum relief rate and back pressure at the relief valve to be higher than the allowable values. The block valve is located between the C3 desuperheater and the C3 condenser after the recycle line take-off point. A proposed solution for minimizing the potential for release is to provide a modulating relief valve as a bypass around the block valve. The set point for the bypass relief valve is lower than that of the relief valve which releases into the flare header at the discharge of C3 compressor. The dynamic response of the pertinent system variables to the closure of the block valve over a period of 15 seconds in presence of the bypass relief valve is shown in Figures 8 to 12. The response in Figure 8 shows the flow rate through the bypass relief valve as % of the initial flow before the closure of the block valve. The C3 compressor discharge pressure in Figure 9, as % of the initial discharge pressure at time zero, shows that the bypass valve is able to maintain the discharge pressure below the relief valve set pressure causing the relief valve to the flare header to remain closed. The C3 and compression power, as % of their respective initial values at time zero, are shown in Figure 1. In this case the gas turbines had enough spare power to avoid trip during the power peaks observed in the transient response. The dynamic response of the anti-surge system in preventing each of the four stages of the C3 compressor from surge is shown in Figures 11 and 12. The simulation results indicate that the transient response of the system stabilizes after about 1 minutes and the C3 compressor is able to operate through the bypass around the closed block valve, although less efficiently and at a higher discharge pressure and consequently higher temperature levels. Thus, the overall dynamic response of the system validates the proposed design modification of using a modulating relief valve as a bypass around the block valve in eliminating the potential for relief due to the inadvertent D.3 5
6 closure of the block valve. The dynamic simulation analysis of the system was also used to determine the appropriate size of the bypass relief valve. flow - % initial C3 Compressor Blocked Outlet 12 2 block valve bypass rv Figure 8 C3 discharge P - % initial C3 Compressor Blocked Outlet rv set pressure Figure 9 power - % initial C3 Compressor Blocked Outlet C3 Figure 1 anti surge valve - % open C3 Compressor Blocked Outlet LP 2 Figure 11 MP D.3 6
7 anti surge valve - % open C3 Compressor Blocked Outlet HP 2 Figure 12 HHP Inadvertent Closure of Block Valve at the Outlet of C3 Receiver Another major failure scenario with potential for a significant release to the flare header is the inadvertent closure of the block valve at the outlet of the C3 receiver. The release would occur if the C3 receiver and condenser become filled with liquid before depletion of liquid C3 inventory from the propane vaporizers. The dynamic response of the system to such a failure scenario is depicted in Figures 13 to 18. The propane condenser gets completely flooded in less than 4 minutes after the closure of the block valve and causes the release to occur. The maximum relief rate and back pressure at the critical relief valve, shown in Figures 13 and 14 respectively, are essentially the same as the maximum allowable values, i.e., %. The C3 compressor discharge pressure, as % of the initial discharge pressure at time zero, is shown in Figure 15. The C3 and compression power, as % of their respective initial values at time zero, are shown in Figure 16. The dynamic response of the anti-surge system in preventing each of the four stages of the C3 compressor from surge is shown in Figures 17 and 18. The dynamic simulation response confirmed the current design of the relief and flare header system to be adequate in handling the relief load associated with this upset scenario assuming enough spare power is available. If not, the compressor will overload and trip shortly on or after the initial relief. An alternative to avoiding such a trip would be a modulating relief valve bypass around the block valve. D.3 7
8 flow - % max 12 2 relief valve flare tip rv back pressure - % max 12 2 Figure 13 Figure 14 C3 discharge P - % initial rv set pressure 11 9 power - % initial C3 Figure 15 Figure 16 anti surge valve - % open 2 LP MP anti surge valve - % open 2 HP HHP Figure 17 Figure 18 D.3 8
9 HYDRAULIC SURGE ANALYSIS OF THE LNG LOADING SYSTEM A hydraulic surge analysis of the LNG loading system was conducted to determine the need for pressure surge dampening equipment to maintain the surge pressures below the pipeline design pressure. The system comprised of several LNG storage tanks and loading pumps and dual LNG loading lines from the storage tanks to the LNG loading jetty. The study involved evaluation of several potential failure scenarios. One of the potential worst case scenarios considered activation of an emergency trip due to the closure of the trip valves at the LNG loading jetty with a subsequent trip of all loading pumps except one in each tank failing to trip. The emergency trip initiates a simultaneous closure of the trip valves at the jetty (with a closure time of 5 seconds) and the trip valves at the plant boundary (with a closure time of 15 seconds). The closure profiles of the trip valves and associated surge pressure profiles are shown in Figures 19 and 2. The hydraulic transient response showed formation of vapor cavities at the emergency trip valves located at the jetty and certain high elevations in the loading lines. This results in spikes in pressure profile, such as the one seen around 16 seconds in Figure 2 due to the collapse of the vapor cavity at the jetty trip valves. The hydraulic surge study determined that pressure surge dampening equipment was not required for the LNG loading system. 12 Hydraulic Surge Analysis pressure (% max) valve (% open) 12 Hydraulic Surge Analysis pressure (% max) valve (% open) % value Emergency Trip Valves - Plant % value Emergency Trip Valves - Jetty time (sec) Figure time (sec) Figure 2 OPTIMUM DESIGN OF THE C3 CONDENSER SIZE The LNG plant simulation model is an effective tool for optimizing the sizes of the C3 and compressor discharge and inter-stage coolers and C3 vaporizers. Results from an LNG plant study conducted for optimizing the C3 condenser size for a fixed total available power from the C3 and gas turbines and helper motors are shown in Figures 21 and 22. A plot of LNG production capacity versus condenser size is shown in Figure 21. Both the LNG production capacity and the condenser area are shown as % of the base design case values. The LNG production capacity increases and the rate of increase in LNG production capacity represented by the slope of the curve decreases with increasing C3 condenser area. Plots of variations in C3 and compression power, as % of the total fixed available power, are shown in Figure 22. The C3 compression power D.3 9
10 requirement decreases while the compression power requirement increases with increasing C3 condenser area. Based on the above information, an economic analysis was performed to determine the most cost effective size of the C3 condenser. C3 Condenser Size Optimization 14 C3 Condenser Size Optimization LNG prod - % base design power - % total C condenser size - % base design Figure condenser size - % base design Figure 22 SENSITIVITY OF LNG PRODUCTION TO VARIATIONS IN COMPRESSOR PERFORMANCE CURVES The compressor performance curves available during the initial process design of an LNG project furnished by compressor vendors are based on preliminary information. Since the compressor performance curves affect the LNG production capacity, it is worthwhile to assess the sensitivity of LNG production to variations in head-flow performance curves for each stage of the C3 and compressors. This information is very helpful to compressor vendors in optimizing the compressor performance. The LNG plant simulation model provides an effective tool for conducting a study of this type. Results from an LNG plant study on the sensitivity of LNG production to variations in the head-flow performance curve for the HHP stage of the C3 compressor are provided in Figures 23 and 24. The analysis is based on a fixed total available power from the C3 and gas turbines and helper motors. The effect of (+/-) 1% variations in the head value for the HHP stage on the LNG production capacity, as % of base design case value, is shown in Figure 23. The LNG production capacity decreases with an increase in the HHP stage head. Plots of variations in C3 and power, as % of total fixed available power, are shown in Figure 24. These plots show that the C3 compression power requirement increases while the compression power requirement decreases with an increase in the HHP stage head. Similar information developed for each stage of the C3 and compressors can then be furnished to compressor vendors for use in their own design optimization effort. D.3 1
11 LNG prod - % base design Sensitivity to Variations in Head- Flow Performance Curve C3 HHP head - % base design Figure 23 power - % total Sensitivity to Variations in Head- Flow Performance Curve C3 HHP head - % base case Figure 24 C3 CONCLUSIONS State-of-the-art modeling tools developed by Fluor Daniel are being used in the performance of dynamic and steady state simulation studies in LNG plant design. These studies are very helpful in addressing a multitude of process design issues during various phases of LNG projects including basic design, detailed engineering, and plant startup and operation. The studies result in improved, cost effective and reliable design of LNG plants. D.3 11
DYNAMICS OF BASELOAD LIQUEFIED NATURAL GAS PLANTS ADVANCED MODELLING AND CONTROL STRATEGIES
DYNAMICS OF BASELOAD LIQUEFIED NATURAL GAS PLANTS ADVANCED MODELLING AND CONTROL STRATEGIES Dr. Matthew J. Okasinski, P.E. Principal Engineer Air Products and Chemicals, Inc. Allentown, Pennsylvania, USA
More informationLARGE CAPACITY LNG TRAINS TRAINS GNL DE GRANDE CAPACITE
LARGE CAPACITY LNG TRAINS TRAINS GNL DE GRANDE CAPACITE Marc Le Métais Jean-Claude Garcel Christian Bladier Exploration & Production TOTAL Paris, France ABSTRACT The capacity of natural gas liquefaction
More informationMLNG DUA DEBOTTLENECKING PROJECT
MLNG DUA DEBOTTLENECKING PROJECT Yahya Ibrahim Senior General Manager Malaysia LNG Malaysia yahyai@petronas.com.my Tariq Shukri LNG Consultant Foster Wheeler Energy Limited Reading, U.K. Tariq_shukri@fwuk.fwc.com
More informationBASIC DESIGN OF PYEONGTAEK LNG RECEIVING TERMINAL-II OF KOREA GAS CORPORATION LA CONCEPTION DE BASE DU TERMINAL METHANIER PYEONGTAEK-II
BASIC DESIGN OF PYEONGTAEK LNG RECEIVING TERMINAL-II OF KOREA GAS CORPORATION LA CONCEPTION DE BASE DU TERMINAL METHANIER PYEONGTAEK-II Youngsoon Sohn Youngmyung Yang Insoo Yoon Sunghee Choi Gunhyung Choi
More informationPROPANE PRECOOLING CYCLES FOR INCREASED LNG TRAIN CAPACITY CYCLES DE PREREFROIDISSEMENT AU PROPANE POUR DES CAPACITES AUGMENTEES DE PRODUCTION DE GNL
PROPANE PRECOOLING CYCLES FOR INCREASED LNG TRAIN CAPACITY CYCLES DE PREREFROIDISSEMENT AU PROPANE POUR DES CAPACITES AUGMENTEES DE PRODUCTION DE GNL Henri Paradowski Gas Processing Technology Manager
More informationTURBO-EXPANDER TECHNOLOGY DEVELOPMENT FOR LNG PLANTS DEVELOPPEMENT DE LA TECHNOLOGIE DES TURBO- EXPANSEURS POUR LES CENTRALES DE GNL
TURBO-EXPANDER TECHNOLOGY DEVELOPMENT FOR LNG PLANTS DEVELOPPEMENT DE LA TECHNOLOGIE DES TURBO- EXPANSEURS POUR LES CENTRALES DE GNL Chen-Hwa Chiu, Ph.D., P.E. Technology Advisor, LNG & Gas Processing
More informationEnhancement of LNG Propane Cycle through Waste Heat Powered Absorption Cooling
Enhancement of LNG Propane Cycle through Waste Heat Powered Absorption Cooling A. Mortazavi 1, P. Rodgers 2, S. Al-Hashimi 2, Y. Hwang 1 and R. Radermacher 1 1 Department of Mechanical Engineering, University
More informationOPTIMUM COMPRESSOR CONTROLS FOR CLOSED LOOP REFRIGERATION
OPTIMUM COMPRESSOR CONTROLS FOR CLOSED LOOP REFRIGERATION William P. Schmidt Janet Firley Mitchell Matthew J. Okasinski Jeremy D. Beard Air Products and Chemicals Abstract This paper discusses compressor
More informationSynergies between process energy efficiency and relief loads
Synergies between process energy efficiency and relief loads Mary Kay O Connor Process Safety Center 2008 Symposium Rob Brendel Jacobs Consultancy Inc. (Chicago) Petroleum, Chemicals & Energy Practice
More informationGASTECH 2OO2. Doug Yates, LNG Operations Coordinator, Phillips Petroleum Company
PROGRAMME GASTECH 2OO2 Doug Yates, LNG Operations Coordinator, Phillips Petroleum Company DOUG YATES is currently the Darwin LNG Operations Manager for the Darwin LNG project in Australia. Prior to assuming
More informationApplying Dynamic Process Simulations Toward Flaring Reduction
Applying Dynamic Process Simulations Toward Flaring Reduction White Paper Siemens AG 2018, All rights reserved 1 Dynamic process simulation has traditionally been a tool of process engineers and process
More informationDynamic Simulation: a Tool for Advanced Design and Operating Behaviour Prediction
A publication of CHEMICAL ENGINEERING TRANSACTIONS VOL. 57, 2017 Guest Editors: Sauro Pierucci, Jiří Jaromír Klemeš, Laura Piazza, Serafim Bakalis Copyright 2017, AIDIC Servizi S.r.l. ISBN 978-88-95608-48-8;
More informationGastech Singapore October Capital Cost and Efficiency Data for the ZR-LNG Dual Methane Expander Liquefaction Technology
Gastech Singapore October 2015 Capital Cost and Efficiency Data for the ZR-LNG Dual Methane Expander Liquefaction Technology Authors: GW Howe, GF Skinner, AD Maunder Presenter: GW Howe Introduction LNG
More informationCONVERTING DOMINION COVE POINT LNG INTO BIDIRECTIONAL FACILITY
CONVERTING DOMINION COVE POINT LNG INTO BIDIRECTIONAL FACILITY Pascal Bocherel, Jim Strohman, Juan Martinez Dominion Cove Point LNG, LP Brett Wink, Kamal Shah, John Ray IHI E & C International Corporation
More informationMITIGATION OF SEASONAL PRODUCTION LOSS FOR THREE PARALLEL 4.7MMTPA
17 th INTERNATIONAL CONFERENCE & EXHIBITION ON LIQUEFIED NATURAL GAS (LNG 17) 17 th INTERNATIONAL CONFERENCE & EXHIBITION MITIGATION OF SEASONAL PRODUCTION LOSS FOR THREE PARALLEL 4.7MMTPA
More informationThe following sub-systems are provided and the integration of these is described below:
The following sub-systems are provided and the integration of these is described below: Pretreatment Plant The Pretreatment Plant typically comprises an amine system for gas sweetening and a molecular
More informationReliquification of Boil of Gas by using BOG Compressor
Reliquification of Boil of Gas by using BOG Compressor Chetan Patil 1, Prasad Bhosale 2 1 Chetan Patil,Student, Mechanical Department, SKN COE Pune, chetanpatil2696@gmail.com 2 Prasad Bhosale, Asst. Professor,
More informationENERGY MANAGEMENT INITIATIVE AT PETRONAS LNG COMPLEX
ENERGY MANAGEMENT INITIATIVE AT PETRONAS LNG COMPLEX AUTHORS: ABDUL HALIM CHE ABAS AZMI ABD RAHMAN FRANKY BUDIT OMAR TECHNICAL SERVICES DEPARTMENT MALAYSIA LNG SDN BHD Page 1 of 11 TABLE OF CONTENTS 1.0
More informationME ENGINEERING THERMODYNAMICS UNIT III QUESTION BANK SVCET
1. A vessel of volume 0.04m 3 contains a mixture of saturated water and steam at a temperature of 250 0 C. The mass of the liquid present is 9 kg. Find the pressure, mass, specific volume, enthalpy, entropy
More informationPreface to the First Edition Preface to the Second Edition. Acknowledgment
Dedication Preface to the First Edition Preface to the Second Edition Forewords Acknowledgment iii xiii xv xvii xix Chapter 1 Introduction to Pipeline Systems 1 1.1 Introduction 1 1.2 Liquid Pipelines
More informationEfficacité supérieure Coût inférieur Plus grande fiabilité et robustesse. PO-6.1
AN ADVANCED CRYOGENIC EXPANDER FOR NATURAL GAS LIQUEFACTION PLANTS AMELIORATION DES PROCEDES DE LIQUEFACTION DE GAZ NATUREL PAR UTILISATION DE TURBINES HYDRAULIQUES S. Gopalakrishnan Pump Division Flowserve
More informationUNIQUE DESIGN CHALLENGES IN THE AUX SABLE NGL RECOVERY PLANT
UNIQUE DESIGN CHALLENGES IN THE AUX SABLE NGL RECOVERY PLANT Presented at the 81 st Annual Convention of the Gas Processors Association March 11, 2002 Dallas, Texas Joe T. Lynch, P.E. Ortloff Engineers,
More informationCO 2 RECOVERY FROM CO 2 REMOVAL UNIT AT GL1Z PLANT
CO 2 RECOVERY FROM CO 2 REMOVAL UNIT AT GL1Z PLANT Hocine Friha Chemical Engineer Technical Department GL1Z/ Sonatrach Bethioua, Oran, Algeria hfriha@avl.sonatrach.dz ABSTRACT Algeria which has ratified
More informationADVANCED PROCESS CONTROL QATAR GAS ONE YEAR EXPERIENCE
ADVANCED PROCESS CONTROL QATAR GAS ONE YEAR EXPERIENCE Bouchebri El-Hadi Senior Process Engineer Benmouley Abdelkader Head of Process Qatar Liquefied Gas Company Limited. Ras Laffan Industrial Area, Doha,
More informationCOMPARISON OF ENERGY EFFICIENCY BETWEEN VARIABLE AND FIXED SPEED SCROLL COMPRESSORS IN REFRIGERATING SYSTEMS
COMPARISON OF ENERGY EFFICIENCY BETWEEN VARIABLE AND FIXED SPEED SCROLL COMPRESSORS IN REFRIGERATING SYSTEMS A. BENAMER, D. CLODIC Ecole des Mines de Paris, Centre d Energétique, 6, bd Saint-Michel 75272
More informationLow Emissions gas turbine solutions
Turbomachinery and Process Solutions Low Emissions gas turbine solutions M.Santini/ M.Baldini 22 March, 2018 Green strategy beyond GT Flange to Flange NOx and CO Emissions reduction CO2 footprint reduction
More informationAppendix 1-A Well Testing
Appendix 1-A Well Testing FLOW TESTING PURPOSE Flow testing is used to determine the performance of oil and gas wells and their economic potential. Various tests will be done to determine the amount of
More informationDETERMINING THE MAXIMUM LNG PRODUCTION RATE BY PROCESS SIMULATION MODELLING OF LOW TEMPERATURE NATURAL GAS SEPARATION UNIT
DETERMINING THE MAXIMUM LNG PRODUCTION RATE BY PROCESS SIMULATION MODELLING OF LOW TEMPERATURE NATURAL GAS SEPARATION UNIT Ewa Ciesielczyk, Oil and Gas Institute, Kraków, Poland Jan Rudnicki, Branch of
More informationCONTROL SOLUTIONS DESIGNED TO FIT RIGHT IN. Energy Control Technologies
Corporate Capabilities CONTROL SOLUTIONS DESIGNED TO FIT RIGHT IN Maximizing your plant s efficiency with control systems built to fit your needs exactly. Energy Control Technologies E nergy Control Technologies
More informationTitle slide. LNG Technology. Compiled by PD.Supriyadi
Title slide LNG Technology Compiled by PD.Supriyadi 1 What is LNG? Colorless, odorless, non toxic hydrocarbon in very low temperature liquid form (cryogenic) Mainly (90% plus) is Methane, the lightest
More information20/06/2011 Seminar on Geothermal Exploitation Santiago de Chile
Contents Power Plants Steam Power plants Binary Power plants Geothermal Power Plants Single flash systems Binary systems 1 Equipment Well head Gathering piping system Steam separators and moisture separators
More informationON THE OPTIMIZATION OF REFRIGERATION MACHINERY
GÖRAN WALL Exergy Studies, Solhemsgatan 46, SE-431 44, Mölndal, Sweden, Email: Goran.Wall@exergy.se published in International Journal of Refrigeration Vol. 14., pp. 336-340. 1991. Abstract. We present
More informationExploring the Design Space with System Simulation to Manage Increasing Thermal Loads on Aircraft Fuel Systems
Exploring the Design Space with System Simulation to Manage Increasing Thermal Loads on Aircraft Fuel Systems Today s modern military fighter jets are like a flying thermos bottle according to Steve Iden,
More informationLNG lifecycle dynamic modeling: From process design verification to support operations
LNG lifecycle dynamic modeling: From process design verification to support operations Leonardo Carpio Houston, 20th March 2018 Agenda OTS Lifecycle dynamic modeling approach Motivation Targets and schedule
More informationThere are many cryogenic
Tray revamp for demethaniser ethane recovery As a first step in an ethane extraction plant s operational improvement plan, a tray revamp was performed to improve both tray efficiency and ethane recovery
More informationNatural Gas Processing Unit Modules Definitions
Natural Gas Processing Unit Modules Definitions Alberta Climate Change Office Draft Version 1.0 December 2018 1 2 3 4 5 6 7 8 9 10 11 12 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35
More informationThermodynamics: An Engineering Approach, 6 th Edition Yunus A. Cengel, Michael A. Boles McGraw-Hill, 2008
Thermodynamics: An Engineering Approach, 6 th Edition Yunus A. Cengel, Michael A. Boles McGraw-Hill, 2008 Chapter 5 MASS AND ENERGY ANALYSIS OF CONTROL VOLUMES SUMMARY 1 CONSERVATION OF MASS Conservation
More informationModular Oil & Gas Equipment Onshore & Offshore
Modular Oil & Gas Equipment Onshore & Offshore Separators & Desalters AI Energy Solutions onshore and offshore oil process solutions offer innovative technologies packaged with global project management
More informationChiller plant optimization
Chiller plant optimization CLEANROOM Terrence Morris & Steve Blaine PE, CH2M HILL, Oregon, USA ABSTRACT Outside of the process tools themselves, the chilled water plant is typically the single largest
More informationAP1000 European 15. Accident Analysis Design Control Document
15.2 Decrease in Heat Removal by the Secondary System A number of transients and accidents that could result in a reduction of the capacity of the secondary system to remove heat generated in the reactor
More informationPath Introductory Module to Fundamentals of 01 Oil & Gas Industry. No. Course Title Duration Dates 01 Introductory Module to Fundamentals
Introductory Module to Fundamentals of Oil & Gas Industry Duration Dates Introductory Module to Fundamentals w Feb-Apr 28 of Oil & Gas Industry Sep-Nov 28 14 15 16 17 18 19 20 Process Training Program
More informationLarge University Central Chiller Plant Design Considerations
Carrier Engineering Newsletter Volume 5, Issue 3 Large University Central Chiller Plant Design Considerations Large campus chilled water plants have unique constraints and need careful evaluation for successful
More informationOptimising. the LNG process. The rapidly expanding global LNG industry continues. Projects
Optimising the LNG process John Baguley, Liquefied Natural Gas Ltd, Australia, outlines the benefits of an innovative liquefaction process technology for mid scale LNG projects. The rapidly expanding global
More informationBrazed Aluminum Heat Exchangers (BAHX) for Optimisation of Natural Gas Liquefaction Processes. Gastech 2017
Brazed Aluminum Heat Exchangers (BAHX) for Optimisation of Natural Gas Liquefaction Processes Authors: Doug Ducote / Paul Shields Introduction Gastech 2017 Brazed aluminum heat exchangers (BAHX), also
More informationAtlantic LNG Train 4 The World s Largest LNG Train
Atlantic LNG Train 4 The World s Largest LNG Train Tony S. Diocee Project Engineering Manager, Trinidad LNG Project Atlantic LNG Company of Trinidad & Tobago Phil Hunter LNG Group Manager Petroleum & Chemicals
More informationA Discussion of Natural Gas Pipeline System Efficiency. Gas/Electric Partnership Houston, Texas February 11, 2010
A Discussion of Natural Gas Pipeline System Efficiency Gas/Electric Partnership Houston, Texas February 11, 2010 1 Pipeline System Efficiency Discussion Points Pipeline Goals Efficiency Metrics Compressor
More informationDYNAMIC MODELING OF THE ISAB ENERGY IGCC COMPLEX
DYNAMIC MODELING OF THE ISAB ENERGY IGCC COMPLEX F. Pisacane R. Domenichini L. Fadabini Foster Wheeler Italiana S.p.A. Via Caboto 1 20094 CORSICO, Italy Abstract During the execution of detailed engineering
More informationP. Heyl, H. Quack, Technische Universität Dresden, Lehrstuhl für Kälte- und Kryotechnik, Dresden 01062, Germany
FREE PISTON EXPANDER-COMPRESSOR FOR CO 2 DESIGN, APPLICATIONS AND RESULTS P. Heyl, H. Quack, Technische Universität Dresden, Lehrstuhl für Kälte- und Kryotechnik, Dresden 01062, Germany ABSTRACT The range
More informationCarbon Capture Options for LNG Liquefaction
Carbon Capture Options for LNG Liquefaction ME-Tech 25 January 2011, Dubai Chris Sharratt Manager, Midstream Business Solutions Group Images: Courtesy of Woodside Energy Ltd Outline LNG liquefaction sources
More informationAREN 2110: Thermodynamics Spring 2010 Homework 7: Due Friday, March 12, 6 PM
AREN 2110: Thermodynamics Spring 2010 Homework 7: Due Friday, March 12, 6 PM 1. Answer the following by circling the BEST answer. 1) The boundary work associated with a constant volume process is always
More informationPrecooling strategies for efficient natural gas liquefaction
Originally appeared in: September/October 217, pgs 19-29. Used with permission. SPECIAL FOCUS: LNG TECHNOLOGY Precooling strategies for efficient natural gas liquefaction G. KRISHNAMURTHY, M. J. ROBERTS
More informationEBARA INTERNATIONAL CORPORATION Cryodynamics Division. Cryogenic Turbine Expanders. cryodynamics. Cryogenic Expanders for Liquefied Gas
EBARA INTERNATIONAL CORPORATION Cryodynamics Division Cryogenic Turbine Expanders cryodynamics Cryogenic Expanders for Liquefied Gas Who we are Liquefaction EBARA International Corporation, Cryodynamics
More informationModelica-Based Heat Pump Model for Transient and Steady-State Simulation Using Low-GWP Refrigerants Paper 2264
Modelica-Based Heat Pump Model for Transient and Steady-State Simulation Using Low-GWP Refrigerants Paper 2264 Jiazhen Ling, Abdullah Alabdulkarem, Hongtao Qiao, Vikrant Aute (vikrant@umd.edu), Reinhard
More informationAPPLICATION OF DYNAMIC SIMULATION FOR DESIGN AND COMMISSIONING OF LNG PLANTS (EXPERIENCE IN MLNG TIGA PROJECT)
APPLICATION OF DYNAMIC SIMULATION FOR DESIGN AND COMMISSIONING OF LNG PLANTS (EXPERIENCE IN MLNG TIGA PROJECT) APPLICATION D UNE SIMULATION DYNAMIQUE POUR LA CONCEPTION ET LA COMMISSION D USINES DE GNL
More informationDYNAMIC SIMULATION OF A PROTON EXCHANGE MEMBRANE FUEL CELL SYSTEM FOR AUTOMOTIVE APPLICATIONS
DYNAMIC SIMULATION OF A PROTON EXCHANGE MEMBRANE FUEL CELL SYSTEM FOR AUTOMOTIVE APPLICATIONS R. A. Rabbani 1 and M. Rokni 2 1. Technical University of Denmark, Kgs. Lyngby, Denmark; email: raar@mek.dtu.dk
More informationTotal Midstream Solutions in Gas Processing/Treating and Crude Oil Handling
Total Midstream Solutions in Gas Processing/Treating and Crude Oil Handling COMPLETE ENGINEERED SOLUTIONS BCCK Engineering helps generate revenue BCCK Engineering Complete Engineered Solutions BCCK Engineering,
More informationQualitative Phase Behavior and Vapor Liquid Equilibrium Core
2/22/2017 Qualitative Phase Behavior and Qualitative Phase Behavior Introduction There are three different phases: solid, liquid, and gas (vapor) Energy must be added to melt a solid to form liquid If
More informationSIMPACK - MODEL DEVELOPMENT PACKAGE FOR POWER PLANTS
SIMPACK - MODEL DEVELOPMENT PACKAGE FOR POWER PLANTS 1.0 OVERVIEW SIMPACK is a totally integrated set of simulation software development modules for power plants. It is template based modeling tool and
More informationMitigating Emissions and Maintenance Constraints with Flare Consolidation
Mitigating Emissions and Maintenance Constraints with Flare Consolidation White Paper Effectively controlling change in a plant environment results in a cumbersome process with an inefficient paper-based
More informationSteam balance optimisation strategies
Steam balance optimisation strategies Publicado en Chemical Engineering, Noviembre 2002 Background Optimising a steam balance in a plant with several steam mains pressures is not always a simple intuitive
More informationDESIGN AND OPERATING EXPERIENCE FOR ANADARKO S LANCASTER FACILITY
DESIGN AND OPERATING EXPERIENCE FOR ANADARKO S LANCASTER FACILITY Presented at the 95 th Annual Convention of the Processors Association April 11, 2016 New Orleans, Louisiana Joe T. Lynch, P.E. Ortloff
More informationEnergy. vecta. Forward Thinking
Our people have expertise that has centred around the Energy Industry in Australia, with skills in the development of green field and brown plants. Our people have core competencies in the following areas:
More informationEffects of flow behavior on the design of transient operation scenarios
Effects of flow behavior on the design of transient operation scenarios *Jakyung Kim 1) and Yutaek Seo 2) 1), 2) Division of Ocean Systems Engineering, KAIST, Daejeon 305-600, Korea 1) kjkwkrud@kaist.ac.kr
More informationLNG PROCESS USES AERODERIVATIVE GAS TURBINES AND TANDEM COMPRESSORS
17 th INTERNATIONAL CONFERENCE & EXHIBITION ON LIQUEFIED NATURAL GAS (LNG 17) 17 th INTERNATIONAL CONFERENCE & EXHIBITION ON LIQUEFIED NATURAL GAS (LNG 17) LNG PROCESS USES AERODERIVATIVE GAS TURBINES
More informationFluid Mechanics, Heat Transfer, and Thermodynamics. Design Project. Production of Acetone
Fluid Mechanics, Heat Transfer, and Thermodynamics Design Project Production of Acetone We are investigating the feasibility of constructing a new, grass-roots, 15,000 metric tons/year, acetone plant.
More informationME 215. Mass and Energy Analysis of Control Volumes CH-6 ÇANKAYA UNIVERSITY. Mechanical Engineering Department. Open Systems-Control Volumes (CV)
ME 215 Mass and Energy Analysis of Control Volumes CH-6 ÇANKAYA UNIVERSITY Mechanical Engineering Department Open Systems-Control Volumes (CV) A CV may have fixed size and shape or moving boundaries Open
More informationYokogawa Corporation of America Receives Analyzer Systems and Shelters Order from Freeport LNG
PRESS RELEASE Yokogawa Corporation of America 12530 West Airport Blvd. Sugar Land, TX 77478 (800) 888-6400 Contact Us FOR IMMEDIATE RELEASE Date: August 8, 2016 Contact Phone: (800) 888-6400 Release #:
More informationModularity Approach of the Modular Pebble Bed Reactor (MPBR)
Modularity Approach of the Modular Pebble Bed Reactor () Marc Berte Professor Andrew Kadak Massachusetts Institute of Technology Nuclear Engineering Department Nuclear Energy Research Initiative Grant
More informationOMESOL. A Potential Hub To Deliver Dynamic Professionals OCTAGON MANAGEMENT & ENGINEERING SOLUTIONS.
OMESOL A Potential Hub To Deliver Dynamic Professionals OCTAGON MANAGEMENT & ENGINEERING SOLUTIONS Aspen Hysys For Oil & Gas People Objectives Learn to build, navigate and optimize process simulations
More informationHow to Evaluate an Existing NGL Recovery Plant Before Finalizing a Process Retrofit Design
How to Evaluate an Existing NGL Recovery Plant Before Finalizing a Process Retrofit Design GPA Midstream Convention April 15-18, 2018 Austin, TX USA Daryl R. Jensen, P.E. Daryl.Jensen@ortloff.com Adebola
More information0611C. Valve Group. Intelligent Pressure Relief System Management Solution. Farris Engineering Services
0611C Valve Group Intelligent Pressure Relief System Management Solution Farris Engineering Services iprsm provides a safer plant protecting people, equipment, communities and the environment. iprsm for
More informationSurge Analysis for the Proposed OSIS Augmentation Relief Sewer Tunnel
5 Surge Analysis for the Proposed OSIS Augmentation Relief Sewer Tunnel M. P. Cherian, Ari Pandian, Karen Ridgway and Gregory Barden The City of Columbus, Ohio, submitted a wet weather management plan
More informationFull electrical LNG-plant: Highest availability and energy efficiency trough overall system design
Full electrical LNG-plant: Highest availability and energy efficiency trough overall system design Dr. Edwin Lerch Principal Expert Power System Dynamics Siemens AG Erlangen, Germany edwin.lerch@siemens.com
More informationHow to establish an integrated production management system across the reservoir lifecycle
SPECAL TOPC: RESERVOR MONTORNG How to establish an integrated production management system across the reservoir lifecycle Stian Engebretsen 1* introduces an integrated production management workflow. ntroduction
More informationBest Practice Pump Control
Best Practice Pump Control Contents 1 Introduction 4 General Recommendations 5 2 Eff icient Pumping System Operation 6 3 Types of Control 7 3.1 Stop/start control 7 3.2 Flow control valve 7 3.3 By-pass
More informationLNG Basics for Petroleum Engineers
LNG Basics for Petroleum Engineers Michael Choi Retired 1 To help protect your privacy, PowerPoint has blocked automatic download of this picture. Primary funding is provided by The SPE Foundation through
More informationAn Environmentally Friendly Business
Vapor Recovery Units An Environmentally Friendly Business German Jimenez, Eni Dacion B.V Carlos Plazas, Eni Dacion B.V David Ochoa, PROYNCA ABSTRACT Eni Dacion is currently operating a medium oil field
More informationExecutive Summary. Engineering Report of the: Adaptation of jetties and LNG transfer facilities for loading of bunker vessels in Fos Tonkin
Executive Summary Engineering Report of the: Adaptation of jetties and LNG transfer facilities for loading of bunker vessels in Fos Tonkin index 01 INTRODUCTION page 4 02 GENERAL DESCRIPTION OF THE PROJECT
More informationChE 455 Fall 2001 Major 1. Ethylene Oxide Production
10/19/01 ChE 455 Fall 2001 Major 1 Ethylene Oxide Production Ethylene oxide is a chemical used to make ethylene glycol (the primary ingredient in antifreeze). It is also used to make poly(ethylene oxide),
More informationChandrashekhar Sonwane, David Hanks, Tony Eastland, Ken Tran, Marinelle Peneda, Jeff Mays, and John Vega. September 9-10, 2014
Supercritical CO 2 Turbomachinery Configuration and Controls for a Zero Emission Coal Fired Power Plant: System Off Design & Control of System Transients Chandrashekhar Sonwane, David Hanks, Tony Eastland,
More informationSource Characterization of Ammonia Accidental Releases for Various Storage and Process Conditions
For Presentation at the Air & Waste Management Association s 90 th Annual Meeting & Exhibition, June 8-13, 1997, Toronto, Ontario, Canada 97-MP8.05 Source Characterization of Ammonia Accidental Releases
More informationHydrate Formation in Chevron Mabee Unit for NGL Recovery and CO 2 Purification for EOR. Abstract
Hydrate Formation in Chevron Mabee Unit for NGL Recovery and CO 2 Purification for EOR Abstract In the early 199 s, Chevron installed a new process to recover natural gas liquids (NGLs) from recycled CO
More informationCCS system modelling: enabling technology to help accelerate commercialisation and manage technology risk
10 th ECCRIA 15 September 2014 CCS system modelling: enabling technology to help accelerate commercialisation and manage technology risk Adekola Lawal Senior Consultant, Power & CCS Overview Systems modelling
More informationNatural Gas STAR Methane Challenge Program: Supplementary Technical Information for ONE Future Commitment Option
Natural Gas STAR Methane Challenge Program: Supplementary Technical Information for ONE Future Commitment Option 1 Contents Introduction... 4 Methane Challenge Program Reporting... 4 Emission Sources...
More information2014 GCC Conference - Orlando, FL Sept. 30 Oct. 2, Simulation of a Combined Cycle using Dynsim. Eric Liese Office of Research and Development
2014 GCC Conference - Orlando, FL Sept. 30 Oct. 2, 2014 Simulation of a Combined Cycle using Dynsim Eric Liese Office of Research and Development Mobile App: Please take a moment Check into Session by:
More informationVarying Views. Variable-primary flow chilled-water systems are of. on Variable-Primary Flow WHAT IS VARIABLE-PRIMARY FLOW? >>>
>>> By William P. Bahnfleth, PhD, PE & Eric B. Peyer Varying Views on Variable-Primary Flow C H I L L E D - W A T E R S Y S T E M S Variable -primary flow survey of designers, chiller manufacturers, and
More informationYemen LNG Operational feedbacks
Yemen LNG Operational feedbacks APCI Owners Seminar XI September 2013 1 Yemen LNG - Agenda 1. Yemen LNG general presentation 2. Feedback on Plant restarts optimization 3. Other operational feedbacks 2
More information2. TECHNICAL DESCRIPTION OF THE PROJECT
2. TECHNICAL DESCRIPTION OF THE PROJECT 2.1. What is a Combined Cycle Gas Turbine (CCGT) Plant? A CCGT power plant uses a cycle configuration of gas turbines, heat recovery steam generators (HRSGs) and
More informationTHE USE OF HYDRAULIC TRANSIENT MODELLING IN THE DESIGN OF RESILIENT PIPELINES
THE USE OF HYDRAULIC TRANSIENT MODELLING IN THE DESIGN OF RESILIENT PIPELINES Alistair Hancox, Grant Pedersen Harrison Grierson Consultants Limited ABSTRACT Pressure surges during the start up, shut down,
More informationTEST BENCH FOR COMPARATIVE MEASUREMENT OF ENERGY EFFICIENCY OF VARIABLE AND FIXED SPEED SCROLL COMPRESSOR
TEST BENCH FOR COMPARATIVE MEASUREMENT OF ENERGY EFFICIENCY OF VARIABLE AND FIXED SPEED SCROLL COMPRESSOR A. BENAMER, D. CLODIC E-mail : benamer@cenerg.ensmp.fr Ecole des Mines de Paris, Centre d Energétique,
More informationR13. (12M) efficiency.
SET - 1 II B. Tech I Semester Regular/Supplementary Examinations, Oct/Nov - 2016 THERMAL AND HYDRO PRIME MOVERS (Electrical and Electronics Engineering) Time: 3 hours Max. Marks: 70 Note: 1. Question Paper
More informationHeat Recovery Systems and Heat Exchangers in LNG Applications. Landon Tessmer LNG Technical Workshop 2014 Vancouver
Heat Recovery Systems and Heat Exchangers in LNG Applications Landon Tessmer LNG Technical Workshop 2014 Vancouver Presentation Overview LNG plant arrangement with heat recovery (OSMR Process by LNG Limited)
More informationChapter 5 MASS AND ENERGY ANALYSIS OF CONTROL VOLUMES
Thermodynamics: An Engineering Approach Seventh Edition in SI Units Yunus A. Cengel, Michael A. Boles McGraw-Hill, 2011 Chapter 5 MASS AND ENERGY ANALYSIS OF CONTROL VOLUMES Copyright The McGraw-Hill Companies,
More informationProblems in chapter 9 CB Thermodynamics
Problems in chapter 9 CB Thermodynamics 9-82 Air is used as the working fluid in a simple ideal Brayton cycle that has a pressure ratio of 12, a compressor inlet temperature of 300 K, and a turbine inlet
More informationHOW TO COMPARE CRYOGENIC PROCESS DESIGN ALTERNATIVES FOR A NEW PROJECT
HOW TO COMPARE CRYOGENIC PROCESS DESIGN ALTERNATIVES FOR A NEW PROJECT Presented at the 86 th Annual Convention of the Gas Processors Association March 12, 2007 San Antonio, Texas Joe T. Lynch, P.E. Ortloff
More informationREFRIGERATION CYCLES
REFRIGERATION CYCLES Carnot Cycle We start discussing the well-known Carnot cycle in its refrigeration mode. Figure 2-1: Carnot Cycle In this cycle we define the coefficient of performance as follows:
More informationCANDU Safety #14 - Loss of Heat Sink Dr. V.G. Snell Director Safety & Licensing
CANDU Safety #14 - Loss of Heat Sink Dr. V.G. Snell Director Safety & Licensing 24/05/01 CANDU Safety - #14 - Loss of Heat Sink.ppt Rev. 0 vgs 1 Steam and Feedwater System steam lines have isolation valves
More informationTHE CONCEPT OF INTEGRATED CRYOGENIC ENERGY STORAGE FOR LARGE SCALE ELECTRICITY GRID SERVICES. Finland *corresponding author
THE CONCEPT OF INTEGRATED CRYOGENIC ENERGY STORAGE FOR LARGE SCALE ELECTRICITY GRID SERVICES Sakari Kaijaluoto 1, Markus Hurskainen 1,* and Pasi Vainikka 2 1 VTT Technical Research Centre of Finland, Koivurannantie
More informationOptimal operation of the boil-off gas compression process using a boil-off rate model for LNG storage tanks
Korean J. Chem. Eng., 25(1), 7-12 (2008) SHORT COMMUNICATION Optimal operation of the boil-off gas compression process using a boil-off rate model for LNG storage tanks Myung Wook Shin, Dongil Shin*, Soo
More informationOhio Energy. Workshop G. Best Practices in Energy Efficiency to Help You Reduce Your Energy Spend. Tuesday, February 21, :45 a.m.
Ohio Energy Workshop G Best Practices in Energy Efficiency to Help You Reduce Your Energy Spend Tuesday, February 21, 2017 10:45 a.m. to Noon Principles of Energy Efficiency Ohio Energy Management Conference
More information