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EP2369279A1 - Procédé de refroidissement ou de liquéfaction d'un flux riche en hydrocarbures et installation d'exécution de celui-ci - Google Patents

Procédé de refroidissement ou de liquéfaction d'un flux riche en hydrocarbures et installation d'exécution de celui-ci Download PDF

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Publication number
EP2369279A1
EP2369279A1 EP10002650A EP10002650A EP2369279A1 EP 2369279 A1 EP2369279 A1 EP 2369279A1 EP 10002650 A EP10002650 A EP 10002650A EP 10002650 A EP10002650 A EP 10002650A EP 2369279 A1 EP2369279 A1 EP 2369279A1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
refrigerant
compressor
hydrocarbon
refrigerant mixture
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP10002650A
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German (de)
English (en)
Inventor
Eginhard Berger
Stephan Walther-Longrée
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IMPAC OFFSHORE ENGINEERING GMBH
Original Assignee
Ph-th Consulting AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ph-th Consulting AG filed Critical Ph-th Consulting AG
Priority to EP10002650A priority Critical patent/EP2369279A1/fr
Publication of EP2369279A1 publication Critical patent/EP2369279A1/fr
Withdrawn legal-status Critical Current

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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
    • F25J1/02—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
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant 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
    • F25J1/0002—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
    • F25J1/0047—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
    • F25J1/0055—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 originating from an incorporated cascade
    • 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
    • F25J1/0211—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • 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
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F25J1/0283—Gas turbine as the prime mechanical driver
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general

Definitions

  • the present invention relates to a process for the liquefaction of hydrocarbons rich streams, in particular natural gas, and a plant for carrying out the same.
  • the prior art discloses a large number of different processes for liquefying hydrocarbon-rich streams, such as natural gas.
  • Facilities for carrying out these processes are referred to as either so-called LNG baseload plants, i. H. Installations for the liquefaction of natural gas for the supply of natural gas as primary energy, or designed as so-called peak-shaving installations, d. H. Installations for the liquefaction of natural gas to cover peak demand.
  • LNG baseload systems are operated with refrigeration circuits, with the refrigerant mixtures circulating in the refrigeration circuits consisting of hydrocarbon mixtures.
  • Such mixture cycles are more energy efficient than so-called expander circuits and allow relatively low energy consumption in the case of the large liquefaction capacities of the LNG baseload plants.
  • Such a single-flow method is for example off US 5,535,594 known.
  • the procedure is such that the higher-boiling refrigerant mixture fraction, ie the bottom product of a distillation column, is used for precooling the hydrocarbon-rich stream to be liquefied and the lower-boiling refrigerant mixture fraction and for cooling against itself.
  • the lower boiling refrigerant mixture fraction that is, the top product of the reflux separator, after being precooled by the higher boiling refrigerant mixture fraction, is used for liquefaction and supercooling of the hydrocarbon-rich stream to be liquefied and for cooling against itself.
  • FIG. 1 Another embodiment of the conventional method with a three-stage compressor is shown in FIG. 1 shown. This will be described in detail below.
  • the stream to be liquefied is fed via line 1 to a heat exchanger E1 for precooling and pre-cooled in this against the refrigerant circuit flow to be heated.
  • the thus pre-cooled stream is optionally supplied via line 2 to a separator.
  • a separator In this possibly existing lower-boiling hydrocarbons are removed.
  • the separation of higher-boiling hydrocarbons is done by providing a so-called HHC (heavy hydrocarbon) column, which serves to separate the heavy hydrocarbons and benzene from the hydrocarbon-rich stream to be liquefied.
  • HHC heavy hydrocarbon
  • Such process components are for example in the DE 197 16 415 described; see for example theirs FIG. 2 as well as the corresponding description.
  • those hydrocarbons which would undesirably increase the calorific value of the liquefied stream, in particular natural gas are often removed before liquefaction.
  • the overhead product of the separator is fed via line 3 to a further heat exchanger E2 and liquefied therein against a further partial flow of the refrigerant circuit.
  • the liquefied stream is then fed via line 4 to a further heat exchanger E3 and subcooled therein against a further partial flow of the refrigerant circuit.
  • the liquefied and supercooled stream is withdrawn via line 5 and the storage or further processing, for. As a nitrogen removal, fed.
  • the withdrawn from the heat exchanger E1 via line 6 warm refrigerant (mixture) stream is first fed to a suction container S1.
  • the refrigerant to be compressed is then fed to the first turbocompressor and then fed on the outlet side via line 8 to a radiator E4.
  • This cooler can be operated with sea or cooling water, air or any other suitable cooling medium. The same applies to the other cooler E5 and E6 of the multi-stage cycle compressor.
  • the cooled refrigerant is then supplied via line 9 to the suction container S2. This serves to avoid that at this point of the cycle possibly resulting liquid phase of the refrigerant enters the compressor stage II.
  • Such containers and their use are known per se.
  • the refrigerant is supplied via line 10 to the further compressor stage II, from where it continues to be compressed via line 11 into the cooler E5, where it partially condenses and then enters via line 12 into the third suction S3, which also serves as a separator and the performs the same function as suction cup S2. From there, the refrigerant flow via line 13 of the third compressor stage III is supplied and passes on via line 14 into the cooler E6, partially condensing, and from there into the return separator D1.
  • the bottom product of the separator D1 is supplied via line 26 to pressure reduction in valve d the current in line 12.
  • the bottom product of the separator S3 is passed via line 16 into the heat exchanger E1, cooled there against the entire refrigerant flow and then expanded in the valve a. Then, this relaxed refrigerant fraction is added to the refrigerant fraction exiting via line 25 from heat exchanger E2 before they then enter the heat exchanger E1 together.
  • the top product of the separator D1 is also passed via line 17 in the heat exchanger E1 and there cooled against itself and then enters via line 18 into the separator D2.
  • the bottom product of the separator D2 is passed via line 23 through heat exchanger E2, where it is further cooled against the refrigerant stream 25 and expanded via line 21 in a Joule-Thomson valve b.
  • the expanded stream is mixed with the refrigerant stream 22 from E3. Together they form the refrigerant flow 25 in E2.
  • the top product from separator D2 is passed through the heat exchangers E2 and E3 and thereby further cooled against current 25 and 22, liquefied and supercooled and finally relaxed to display the necessary for the process, the lowest temperature in the valve c. Then, this relaxed refrigerant fraction is passed in countercurrent through the heat exchanger E3, so as to effect on the one hand, the liquefaction of the hydrocarbon-rich stream and the internal cooling of the refrigerant. In doing so, it goes over itself by evaporation and warming from the predominantly liquid to the gas state.
  • this refrigerant fraction is then combined with the bottom product from the separator D2. This was previously cooled via line 23 in the heat exchanger E2 and relaxed in the valve b. After passing through this combined coolant fraction through heat exchanger E2, it is, as already mentioned above, combined with the refrigerant fraction relaxed in valve a and fed to the compressor unit after passing through heat exchanger E1.
  • FIG. 2 shows a further embodiment of this conventional method, in which the heat exchangers E3, E2 and E3 are designed in the form of coiled heat exchanger. This eliminates the lines 22 and 25 FIG. 1 ,
  • the invention relates to a method for operating a multi-stage compressor of a refrigerant circuit, wherein a refrigerant mixture that in at least one of a A plurality of fractions (16, 17, 20, 23) has been passed through the successive heat exchanger sections of at least one heat exchanger, the individual stages of the refrigerant cycle compressor (I, II, III) is at least partially supplied separately on the suction side (6, 6a, 6b) ,
  • the process of the invention has the following advantages. On the one hand, the energy requirement is lower than in the liquefaction and cooling processes of the prior art. As a result, the environmental impact is lower. All heat exchanger stages can be made smaller than in the prior art. This also applies to the compressor and the gas turbine used. As a result, the method according to the invention is generally associated with lower costs than conventional methods of the prior art.
  • refrigerant and “refrigerant circuit” are also used to describe refrigerant mixtures and the mixed refrigerant cycle of the present invention. These include in particular multiphase refrigerant mixtures and refrigerants which consist of one or more different chemical components.
  • a refrigerant mixture can be used which contains a combination of nitrogen, methane, ethane, propane, butane and possibly also pentane.
  • the temperatures in the refrigerant circuit are within the range of the local ambient temperature up to 50 ° C or higher after the compressor stages, down to about -160 ° C or below.
  • the pressure range is approximately between one and 50 bar.
  • mixed refrigerant fraction and “mixed refrigerant stream” or even just “fraction” or “stream” are used synonymously herein. They designate a part of the mono- or multiphase refrigerant mixture in a subsection of the method according to the invention or in a part of the system according to the invention, e.g. a fraction in heat exchanger E1 or heat exchanger E2.
  • heat exchanger section as used herein is meant individual heat exchangers or individual sections (sections) of a heat exchanger that may be located within a generally outwardly insulated enclosure (“cold box”) or individually insulated. This is known to the person skilled in the art. In the following, the terms “heat exchanger section” and “heat exchanger” are also used interchangeably.
  • compressor and “compressor” are used synonymously.
  • cry box is well known in the art.
  • the term refers to an isolated cryogenic apparatus which cools fluids to low temperature levels, e.g. Up to -40 ° C to -190 ° C or below.
  • Joule-Thomson valve By a Joule-Thomson valve is meant a valve through which a liquid, gas or liquid-gas mixture adiabatically expands, which leads to a decrease in temperature.
  • the procedure according to the invention is that the optionally pretreated, hydrocarbon-rich stream to be liquefied, in particular natural gas, is fed to a first heat exchanger E1.
  • a pre-cooling of the stream takes place against the refrigerant.
  • the thus pre-cooled stream is fed to a second heat exchanger E2 and further cooled and liquefied in this against the refrigerant in this heat exchanger.
  • the liquefied stream is fed to a third heat exchanger E3 and subcooled therein against the refrigerant present therein.
  • the thus liquefied and supercooled hydrocarbon-rich stream, in particular natural gas is then fed via a suitable line of its further use, for example, an intermediate storage. This is not shown in detail in the figures. Cooling and liquefaction use the Joule-Thomson effect.
  • the pressure release in the respective heat exchangers can thus be effected according to the invention by means of Joule-Thomson valves or by means of hydraulic expanders in combination with Joule-Thomson valves or by means of two-phase expander.
  • Joule-Thomson valves or by means of hydraulic expanders in combination with Joule-Thomson valves or by means of two-phase expander.
  • Such devices are known per se in the prior art. The latter are for example in the DE 103 55 935 A1 described.
  • the refrigerant which exits the three heat exchanger units E1, E2 and E3, fed to a multi-stage compressor for the refrigerant mixture cycle, in particular three compressor stages I, II and III or even more stages, for. B. includes four, five or six stages.
  • the procedure according to the invention is such that the refrigerant streams emerging from the respective heat exchanger are fed separately to the cycle compressor stages.
  • the refrigerant flows within the cycle compressor ie the part of the system that the individual Compressor, suction container for their protection and required cooler includes, insofar combined with each other, as a refrigerant flow, which has already passed through a compressor stage, with another refrigerant flow, which has not gone through any stage compressor, can be combined. Thereafter, the stream thus combined passes through another downstream compressor stage.
  • the refrigerant flows to the individual stages of the cycle compressor as a whole "at least partially separated" supplied.
  • the streams of the refrigerant leaving the heat exchanger units are in any case not combined as long as at least one stream has not been compressed.
  • the heat exchanger sections E1, E2 and E3 can each be subdivided into further sections, wherein the refrigerant flows are fed in an analogous manner to the likewise further subdivided compressor stages.
  • the bottom product of the (high-pressure) precipitator D1 entering the heat exchanger E1 after cooling is not cooled up against itself and expanded in the valve a, relative to the heat exchanger E1 and the Arrangement of the valve a, is combined with a further refrigerant fraction, but after passage of heat exchanger E1 (for self-cooling and precooling of hydrocarbons rich stream (1)) is combined via line 6 with emerging from the cooler E5 via line 12 and already compressed refrigerant fraction and passed via line 12a into the suction container S3. From there, this combined refrigerant fraction is fed via line 13 to the suction side of the compressor unit III and further compressed.
  • the head product stream 17 exiting from the (high-pressure) precipitator D1 after passing through the heat exchanger E1 in which it is cooled against itself, is conducted into the separator D2 just like in the conventional method, where it is split into two streams which pass over the lines 19 (top product) and 23 (bottom product) are passed into the heat exchanger E2.
  • This combined refrigerant fraction then passes through the second compressor stage II and, as already mentioned above, after further cooling in cooler E5, is combined with the fraction leaving the heat exchanger E1 via line 6.
  • the suction pipe for the refrigerant mixture to the first stage of the refrigerant cycle compressor must be designed with a diameter as large as in the method of the prior art.
  • the refrigerant fractions are first combined after passing through the heat exchangers E3, E2 and E1 and then supplied to the first compressor stage.
  • this also leads to a comparatively greater energy requirement in the subsequent compression and cooling, which is reduced by the method of the present invention due to the separate and feed at colder temperatures.
  • the individual refrigerant fractions are fed to the stages of the refrigerant cycle compressor at a comparatively lower temperature than in the case of the prior art method.
  • the compressor and the cooling capacity (after compression) are lower than in the prior art methods. This is a significant contribution to energy saving, as the energy consumption of the refrigerant cycle compressor regularly represents the largest consumption component in gas liquefaction.
  • the process control according to the invention is also advantageous because the refrigerant fraction passing through the heat exchanger E3 is fed directly back to the compression after exiting via line 22, and not, as in the in FIG. 1 shown prior art, is further passed through the heat exchangers E2 and E1.
  • this refrigerant fraction is largely gaseous, so that the heat exchange in the subsequent heat exchangers E2 and E1 is worse than in the inventive method in which each "fresh" relaxed refrigerant fractions are passed solely through the respective heat exchanger.
  • the heat is exchanged in a much more favorable manner by evaporation of the liquid phase of the refrigerant, whereby the heat exchanger surface, the volume and thus the cost of the heat exchanger can be reduced. also reduces the pressure loss for the refrigeration cycle, which contributes to the further reduction of the power requirement of the cycle compressor.

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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)
EP10002650A 2010-03-12 2010-03-12 Procédé de refroidissement ou de liquéfaction d'un flux riche en hydrocarbures et installation d'exécution de celui-ci Withdrawn EP2369279A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP10002650A EP2369279A1 (fr) 2010-03-12 2010-03-12 Procédé de refroidissement ou de liquéfaction d'un flux riche en hydrocarbures et installation d'exécution de celui-ci

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP10002650A EP2369279A1 (fr) 2010-03-12 2010-03-12 Procédé de refroidissement ou de liquéfaction d'un flux riche en hydrocarbures et installation d'exécution de celui-ci

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105823300A (zh) * 2015-01-06 2016-08-03 中国石化工程建设有限公司 一种低能耗天然气液化方法
DE102015002443A1 (de) * 2015-02-26 2016-09-01 Linde Aktiengesellschaft Verfahren zum Verflüssigen von Erdgas
CN107514871A (zh) * 2016-06-17 2017-12-26 中国石化工程建设有限公司 单压缩机混合冷剂天然气液化系统及方法
EP3951297A4 (fr) * 2019-04-01 2022-11-16 Samsung Heavy Ind. Co., Ltd. Système de refroidissement

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3929438A (en) * 1970-09-28 1975-12-30 Phillips Petroleum Co Refrigeration process
US5535594A (en) 1993-04-09 1996-07-16 Gaz De France (Service National) Process and apparatus for cooling a fluid especially for liquifying natural gas
DE19716415C1 (de) 1997-04-18 1998-10-22 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
US5826444A (en) * 1995-12-28 1998-10-27 Institut Francais Du Petrole Process and device for liquefying a gaseous mixture such as a natural gas in two steps
US20020170312A1 (en) * 1999-12-01 2002-11-21 Reijnen Duncan Peter Michael Offshore plant for liquefying natural gas
DE10355935A1 (de) 2003-11-29 2005-06-30 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
WO2006007278A2 (fr) * 2004-06-23 2006-01-19 Exxonmobil Upstream Research Company Procede de liquefaction de refrigerant mixte

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3929438A (en) * 1970-09-28 1975-12-30 Phillips Petroleum Co Refrigeration process
US5535594A (en) 1993-04-09 1996-07-16 Gaz De France (Service National) Process and apparatus for cooling a fluid especially for liquifying natural gas
US5826444A (en) * 1995-12-28 1998-10-27 Institut Francais Du Petrole Process and device for liquefying a gaseous mixture such as a natural gas in two steps
DE19716415C1 (de) 1997-04-18 1998-10-22 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
US20020170312A1 (en) * 1999-12-01 2002-11-21 Reijnen Duncan Peter Michael Offshore plant for liquefying natural gas
DE10355935A1 (de) 2003-11-29 2005-06-30 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
WO2006007278A2 (fr) * 2004-06-23 2006-01-19 Exxonmobil Upstream Research Company Procede de liquefaction de refrigerant mixte

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105823300A (zh) * 2015-01-06 2016-08-03 中国石化工程建设有限公司 一种低能耗天然气液化方法
CN105823300B (zh) * 2015-01-06 2018-10-16 中国石化工程建设有限公司 一种低能耗天然气液化方法
DE102015002443A1 (de) * 2015-02-26 2016-09-01 Linde Aktiengesellschaft Verfahren zum Verflüssigen von Erdgas
CN107514871A (zh) * 2016-06-17 2017-12-26 中国石化工程建设有限公司 单压缩机混合冷剂天然气液化系统及方法
EP3951297A4 (fr) * 2019-04-01 2022-11-16 Samsung Heavy Ind. Co., Ltd. Système de refroidissement

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