EP2796819B1 - Procédé et appareil pour la liquéfaction de gaz naturel - Google Patents

Procédé et appareil pour la liquéfaction de gaz naturel Download PDF

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Publication number
EP2796819B1
EP2796819B1 EP14165010.1A EP14165010A EP2796819B1 EP 2796819 B1 EP2796819 B1 EP 2796819B1 EP 14165010 A EP14165010 A EP 14165010A EP 2796819 B1 EP2796819 B1 EP 2796819B1
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EP
European Patent Office
Prior art keywords
gas
bar
natural gas
temperature
heat exchange
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EP14165010.1A
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German (de)
English (en)
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EP2796819A2 (fr
EP2796819A3 (fr
Inventor
Osvaldo Del Campo
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GNC Galileo SA
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GNC Galileo SA
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0087—Propane; Propylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/70—Processing device is mobile or transportable, e.g. by hand, car, ship, rocket engine etc.

Definitions

  • the present invention relates generally to the compression and liquefaction of gases, and more particularly to the partial liquefaction of a gas, such as natural gas, on a small scale by utilizing a combined refrigerant and expansion process.
  • Natural gas is a mixture of gases that was formed from fossil remains of plants and animals that are buried deep below the Earth's surface. Natural gas is composed primarily of methane, although it also contains ethane, propane, and traces of other gases. Depending on where it is extracted, it varies between 87%/96% methane with about 1.5% to 5% ethane, and 0.1% to 1.5% propane.
  • Natural gas is a known alternative to combustion fuels such as gasoline and diesel. Much effort has gone into the development of natural gas as an alternative combustion fuel in order to combat various drawbacks of gasoline and diesel including production costs and the subsequent emissions created by the use thereof. As is known in the art, natural gas is a cleaner burning fuel than other combustion fuels.
  • LNG Liquefied Natural Gas
  • LNG is natural gas in its liquid form. In order to liquefy natural gas, it must be cooled. As a liquid, natural gas occupies only 1/600th of the volume of natural gas (at atmospheric pressure) in its gaseous form and thereby allows for more economical and practical transportation over great distances. Natural gas is typically transported in liquid state when vast distances, geological or political conditions do not allow for construction of pipelines.
  • the cascade cycle consists of a series of heat exchangers with the feed gas; each exchange being at successively lower temperatures until the desired liquefaction is accomplished.
  • the levels of refrigeration are obtained with different refrigerants or with the same refrigerant at different evaporating pressures.
  • the cascade cycle is considered to be very efficient at producing LNG as operating costs are relatively low.
  • An additional problem with large facilities is the cost associated with storing large amounts of fuel in anticipation of future use and/or transportation. Not only is there a cost associated with building large storage facilities, but there is also an efficiency issue related therewith as stored LNG will tend to warm and vaporize over time creating a loss of the LNG fuel product.
  • Micro LNG is a natural gas liquefaction plant producing in the range of 50-150 k/tons per year of LNG.
  • the biggest difference between traditional large plants, which produce in excess of 1 million tons per year, and Micro LNG is the end user the product is destined for.
  • the product is produced for international export, where the plant economy of scale is among the most important factors.
  • the distributed production is primarily aimed at local markets, where it is re-gasified and fed as pipeline natural gas or used for local power generation. It includes centrifugal and integrally gear compressors and companders, turbo expander compressors, reciprocating compressors and controllers, which makes this solution very expensive and its adaptability very rigid.
  • the present invention is directed to a method for the liquefaction of natural gas that overcomes the difficulties and drawbacks of the methods of the prior art.
  • the present invention overcomes the deficiencies of the known art and the problems that remain unsolved by providing an easy-to-install and practical method for the liquefaction of natural gas with which it is possible to provide a low scale production of LNG at reasonable costs.
  • the present invention provides a method according to claim 1.
  • a method for liquefying natural gas according to claim 1 furthermore comprising: a pre-treating step for removing impurities such as carbon dioxide, nitrogen, etc., from the natural gas flow taken from a source of unpurified natural gas.
  • the present invention is referred to a method for the liquefaction of natural gas that includes an exclusive high pressure LNG liquefaction cycle for small scale production.
  • This cycle allows the production at very economical costs of up to 20000 Nm3/day of LNG with a very low operating cost and a significantly lower level investment in comparison with any other known facility available in the market.
  • the cycle 100 starts at the inlet 101 of unpurified natural gas.
  • This inlet may come from a gas well, an oil well, a natural gas production pipe, or the like. That gas is pretreated at the treatment device 102 to suit it to liquefaction conditions.
  • This natural gas contains, at this stage, impurities that need to be removed. Some of these impurities may be carbon dioxide, nitrogen, and other gases. These impurities must be removed to make the gas fit for this cycle.
  • the gas Once the gas is purified at 102, it enters into a first high-pressure multi-stage compressor 103. After the stage 103, the gas enters into a heat exchanger 104 after which the mixture of liquid and gaseous natural gas enters a cold box 105 from which the liquefied gas is transferred to a flash liquid/gas separator 106 for its storage 107 and/or transportation 108. Between the cold box and the separator an expansion valve is included to reduce the pressure creating a Joule Thompson effect.
  • An independent propane refrigeration cycle 120 including an additional high-pressure multi-stage 109 and a heat exchange stage 110 helps the general cycle 100 to perform the last liquefaction process in the cold box 105.
  • the natural gas that still remains in the gaseous state in the cold box 105 is then transferred to a booster compressor 111 and a heat exchanger 112 before it is re-injected into the inlet pipe 122 being mixed with the gas incoming from the treatment plant.
  • FIG. 2 shows in more detail the present method 100 for the liquefaction of natural gas.
  • the high-pressure multi-stage compressor 103 is shown in this figure as a three-stage process including a first compression stage 201 for compressing the natural gas coming from the inlet pipe 122 at around 10/11 bar to around 30/35 bar.
  • a first compression stage 201 for compressing the natural gas coming from the inlet pipe 122 at around 10/11 bar to around 30/35 bar.
  • the temperatures rise from around 36 °C to 148 °C; therefore, it is necessary to reduce this temperature drastically for which the gas enters into a first heat exchange stage 202 to cool down the temperature of the gas from 148 °C to 40 °C.
  • a second compression stage 203 starts for compressing the natural gas from around 33 bar at the end of the first stage to around 95 bar, and during which the temperatures rise from 40 °C to 149 °C. Therefore, a second heat exchange stage 204 for cooling down the temperature of the gas from 149 °C to 40 °C is performed.
  • a third compression process 205 is performed for compressing the natural gas from around 95 bar to around 250 bar, and in which the temperatures rise from 40 °C to 136 °C. Therefore, in a heat exchanger 206, a third heat exchange stage cools down the temperature of the gas from 136 °C to 40 °C.
  • the natural gas is at 250 bar and 40 °C. It is then injected into a regeneration cycle 207 that cools down the temperature of the gas from 40 °C to 7 °C keeping the pressure at 250 bar.
  • a first main independent heat exchange cycle 208 cools down the temperature of the gas from 7 °C to -47 °C while pressure is kept at 250 bar.
  • This independent cycle is fed by a propane cycle 120 that includes a compressor 121, a heat exchanger 122, a second compressor 123 and a second heat exchanger 124 that basically liquefies, expands and vaporizes said propane gas.
  • a second main heat exchange cycle 209 cools down the temperature of the gas from -47 °C to -77 °C while pressure is kept at 250 bar.
  • This second main heat exchange cycle 209 uses the energy of the returning gas through line 210 as will be explained in detail below.
  • part of the mass of the natural gas is already in a liquid state.
  • the mix of liquid and gaseous natural gas at -77 °C and 250 bar is expanded in an separator device 211 including an internal thermal expansion valve that reduces the gas pressure from 250 bar to 2 bar.
  • This significant drop in the gas pressure also produces a significant drop in the gas temperature because of the Joule-Thomson effect.
  • the Joule-Thomson expansion describes the temperature change of a gas when it is forced through a valve while kept insulated so that no heat is exchanged with the environment. This procedure is called a throttling process or Joule-Thomson process.
  • this evaporator 211 At the exit of this evaporator 211, around half of the mass of natural gas has been liquefied as it is at -151 °C and 2 bar. It is then collected for further processing (storage of transportation) through a pipe 215. The gaseous portion of the gas at -151 °C and 2 bar is injected through the pipe 210 into the second main heat exchange cycle 209. Because of the temperature difference between the gas returning from pipe 210 (-151 °C) and the gas entering the second main heat exchange cycle 209 at -47 °C, this returning gas helps the heat exchange process. At the exit of said second main heat exchange cycle 209, through pipe 212, said returning gas is at -60 °C and 2 bar.
  • this returning gas Before this returning gas can be incorporated in the aspiration pipe 122, it must be compressed, as the entrance gas is already at 11 bar and this returning gas is at 2 bar. Thus, this returning gas at 37°C and 1.9 bar enters a compressor 216 that raises the gas pressure from 2 bar to 11 bar and the temperature rises from 37 °C to 224 °C. Therefore, before injecting it into the inlet pipe 122 is injected into a heat exchanger 217 that cools it down from 224 °C to 40 °C. Through a pipe 218, this returning gas is finally reincorporated in the circuit and the process may start again.
  • FIG. 3 shows one example of a transportable and compact plant used to perform the liquefaction method of the present invention.
  • the module 300 illustrated in FIG. 3 all the necessary elements are included. Therefore once the inlet gas pipe and the LNG outlet liquid gas are connected the plant is fully operational. Instead of having all the typical complex and expensive means used in the LNG plants of the prior art, this solution provides a flexible, affordable solution for low volumes application.
  • FIG. 3 In the general perspective view of FIG. 3 some of the parts can be distinguished, including a compressor 301, three heat exchangers 302, a GNL module 303, the GNL outlet 304, refrigerating funs 305, two vent chimneys 306 and a display control 307.
  • FIGS. 4-6 show an internal unit of the module of FIG. 3 .
  • the unit includes accumulators 321, a GNL outlet 322, and a propane inlet 323.
  • the heat exchangers 325 of the unit 320 are protected by an external isolating cover 324.
  • the unit also includes a propane outlet 326 and a natural gas outlet 327.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (3)

  1. Procédé pour la liquéfaction de gaz naturel, comprenant :
    prendre du gaz naturel non épuré (101) d'un puits de gaz ;
    pré-traiter le gaz pour retirer les impuretés ;
    réaliser un premier étage de compression (201) pour comprimer le gaz naturel d'environ 10/11 bars à environ 30/35 bars et dans lequel les températures passent de 30/35 °C à 140/150 °C ;
    réaliser une première étape de transfert de chaleur (202) pour refroidir le gaz en portant sa température de 140/150 °C à 40/45 °C ;
    réaliser une seconde compression (203) pour comprimer le gaz naturel d'environ 30/35 bars à environ 90/95 bars et dans laquelle les températures passent de 40/45 °C à 140/150 °C ;
    réaliser une seconde étape de transfert de chaleur (204) pour refroidir le gaz en portant sa température de 140/150 °C à 40/45 °C ;
    réaliser un troisième étage de compression (205) pour comprimer le gaz naturel d'environ 90/95 bars à environ 245/250 bars et durant lequel les températures passent de 40/45 °C à 140/145 °C ;
    réaliser un troisième transfert de chaleur (206) pour refroidir le gaz en portant sa température de 140/145 °C à 40/45 °C ;
    réaliser une étape supplémentaire de transfert de chaleur de régénération (207) pour refroidir le gaz en portant sa température de 40/45 °C à 7/10 °C ;
    réaliser un premier cycle de transfert de chaleur principal indépendant (120/208) pour refroidir le gaz en portant sa température de 7/10 °C à -40/-45 °C tout en maintenant la pression à 250 bars ;
    réaliser un second transfert de chaleur principal (209) pour refroidir le gaz en portant sa température de -40/-45 °C à -75/-80 °C tout en maintenant la pression à 250 bars ;
    passer le gaz à 250 bars et à -75/-80 °C à travers une vanne de Joule-Thomson permettant au flux de se dilater en réduisant ainsi sa température à -150/-155 °C et en réduisant sa pression à 2 bars ;
    stocker le gaz liquéfié (215) ;
    injecter la partie gazeuse du gaz naturel en aval de la vanne de Joule-Thomson (210) à -150 °C et à 2 bars dans le second cycle de transfert de chaleur principal pour faciliter le processus de refroidissement décrit précédemment, augmenter sa température en la passant de -150 à -60 °C ; et par la suite le gaz à -60 °C (212, 213) est injecté dans l'étape de transfert de chaleur de régénération (207) pour faciliter le processus de refroidissement décrit précédemment.
  2. Procédé pour la liquéfaction de gaz naturel selon la revendication 1, dans lequel durant l'étape de pré-traitement, du dioxyde de carbone et/ou de l'azote est retiré du gaz naturel.
  3. Procédé pour la liquéfaction de gaz naturel, comprenant :
    réaliser ladite étape de pré-traitement pour retirer les impuretés telles que le dioxyde de carbone, l'azote etc., du débit de gaz naturel pris d'une source de gaz naturel non épuré ;
    réaliser ledit premier étage de compression pour comprimer le gaz naturel d'environ 11 bars à environ 33 bars et dans lequel les températures passent de 36 à 148 °C ;
    réaliser ladite première étape de transfert de chaleur pour refroidir le gaz en portant sa température de 148 à 40 °C ;
    réaliser ledit second étage de compression pour comprimer le gaz naturel d'environ 33 bars à environ 95 bars et dans lequel les températures passent de 40 à 148 °C ;
    réaliser ladite seconde étape de transfert de chaleur pour refroidir le gaz en portant sa température de 149 à 40 °C ;
    réaliser ledit troisième étage de compression pour comprimer le gaz naturel d'environ 95 bars à environ 250 bars et dans lequel les températures passent de 40 à 136 °C ;
    réaliser ladite troisième étape de transfert de chaleur pour refroidir le gaz en portant sa température de 136 à 40 °C ;
    à 250 bars, réaliser ladite nouvelle étape de transfert de chaleur faisant partie dudit cycle de régénération pour refroidir le gaz en portant sa température de 40 à 7 °C ;
    réaliser ledit premier cycle de transfert de chaleur indépendant principal pour refroidir le gaz en portant sa température de 7 à -47 °C tout en maintenant la pression à 250 bars ;
    réaliser ledit second cycle de transfert de chaleur principal pour refroidir le gaz en portant sa température de -47 à -77 °C tout en maintenant la pression à 250 bars ;
    à 250 bars et -77 °C, le gaz passe à travers une vanne de Joule-Thomson permettant au flux de se dilater en réduisant ainsi sa température à -151 °C et en réduisant sa pression à 2 bars.
EP14165010.1A 2013-04-24 2014-04-16 Procédé et appareil pour la liquéfaction de gaz naturel Active EP2796819B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US13/869,485 US20140318178A1 (en) 2013-04-24 2013-04-24 Method and apparatus for the liquefaction of natural gas

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EP2796819A2 EP2796819A2 (fr) 2014-10-29
EP2796819A3 EP2796819A3 (fr) 2015-12-16
EP2796819B1 true EP2796819B1 (fr) 2018-06-06

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US (1) US20140318178A1 (fr)
EP (1) EP2796819B1 (fr)
AR (1) AR096064A1 (fr)
ES (1) ES2675592T3 (fr)
TR (1) TR201809037T4 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10605522B2 (en) * 2016-09-01 2020-03-31 Fluor Technologies Corporation Methods and configurations for LNG liquefaction
EP3596415A4 (fr) 2017-03-14 2020-07-22 Woodside Energy Technologies Pty Ltd Unité de liquéfaction de gnl conteneurisée et procédé associé de production de gnl
EP4211100A4 (fr) 2020-09-14 2024-02-28 ConocoPhillips Company Procédé et appareil de création d?une petite augmentation de pression dans un courant de gaz naturel
WO2022093762A1 (fr) * 2020-10-26 2022-05-05 JTurbo Engineering & Technology, LLC Procédés et configurations pour la liquéfaction de gnl

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US3292382A (en) * 1964-02-21 1966-12-20 Continental Oil Co Low temperature separation of h2s from hydrocarbon gas
US3323315A (en) * 1964-07-15 1967-06-06 Conch Int Methane Ltd Gas liquefaction employing an evaporating and gas expansion refrigerant cycles
US5327730A (en) * 1993-05-12 1994-07-12 American Gas & Technology, Inc. Method and apparatus for liquifying natural gas for fuel for vehicles and fuel tank for use therewith
KR20080097141A (ko) * 2007-04-30 2008-11-04 대우조선해양 주식회사 인-탱크 재응축 수단을 갖춘 부유식 해상 구조물 및 상기부유식 해상 구조물에서의 증발가스 처리방법
CA2718840A1 (fr) * 2008-04-11 2009-10-15 Fluor Technologies Corporation Procedes et configuration du traitement de gaz d'evaporation dans des installations de regazeification de gnl
GB2469077A (en) * 2009-03-31 2010-10-06 Dps Bristol Process for the offshore liquefaction of a natural gas feed
CA2840723C (fr) * 2011-08-09 2019-10-01 Exxonmobil Upstream Research Company Procede de liquefaction du gaz naturel

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Publication number Publication date
ES2675592T3 (es) 2018-07-11
EP2796819A2 (fr) 2014-10-29
AR096064A1 (es) 2015-12-02
US20140318178A1 (en) 2014-10-30
TR201809037T4 (tr) 2018-07-23
EP2796819A3 (fr) 2015-12-16

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