US3702063A - Refrigeration cycle for the aliquefaction of natural gas - Google Patents

Refrigeration cycle for the aliquefaction of natural gas Download PDF

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Publication number
US3702063A
US3702063A US873964A US3702063DA US3702063A US 3702063 A US3702063 A US 3702063A US 873964 A US873964 A US 873964A US 3702063D A US3702063D A US 3702063DA US 3702063 A US3702063 A US 3702063A
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intercooler
cycle
condensate
natural gas
pressure
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US873964A
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Volker Etzbach
Wolfgang Forg
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Linde GmbH
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Linde GmbH
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    • 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
    • F25J1/0032—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"
    • F25J1/0045—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 vaporising a liquid return 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
    • F25J1/003—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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—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 only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration 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
    • F25J1/0211—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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • ABSTRACT In the liquefaction of natural gas wherein the refrigeration cycle fluid contains natural gas components, and such components are subjected to fractional condensation to obtain different temperature levels of refrigeration, the system is improved by'adjusting the C -C content of cycle fluid and the pressure of at least one intermediate pressure stage of the circulation pressure in such a manner that condensate is formed in the corresponding intercooler of said pressure stage. This condensate is then separated and subjected to heat exchange to utilize its refrigeration values and recirculated to the circulation compressor via an expansion valve. In this way, a substantial concentration of heavy hydrocarbons can be utilized to increase the refrigeration capacity of the refrigeration cycle, but said hydrocarbons do not deleteriously affect the lower temperature levels of refrigeration.
  • the function of the refrigeration cycle is to produce the refrigeration required for liquefying natural gas [depending on climatic conditions having an ambient]. Another object is to provide apparatus for conducting such a process.
  • a refrigeration cycle fluid is advantageously employed which is composed of components also having differing boiling points, as disclosed, for example, by A. P. Kleemenko (Comptes rendus du'Congres du Froid de Copenhague 1959, pp. 34-39).
  • the cycle fluid is then partially condensed in multiple stages, each liquid fraction being separated from the gaseous phase, expanded, vaporized, heated and recycled to the compressor.
  • the components having low boiling points such as methane and nitrogen, yield the refrigeration required at the lowest temperature level whereas the fraction containing ethane and propane yields refrigeration values at an intermediate temperature level.
  • the refrigeration required for the precooling step i.e. for cooling to a temperature corresponding approximately to the boiling point of ammonia at atmospheric pressure (33C.), is produced by the vaporization of a mixture of higher hydrocarbons, such as propane, butane, and higher-boiling compounds.
  • a principal object of this invention is to provide an improved process for the liquefaction of natural gas so that the refrigerating capacity of the cycle fluid is increased without deleteriously affecting the temperature level of the lower temperature refrigerating stages.
  • the resultant warmed gas is recycled to the inlet side of the circulation compressor.
  • the condensate is expanded (pressure-reduced) exclusively of any condensate of the vapor phase separated therefrom in the preceding step; the resultant separated vapor is then recompressed downstream of the intermediate compression stage, and then subjected to multiple stages of condensation, phase separation, and expansion of resultant condensates to produce the required multiple stages of decreasing temperature necessary for liquefying the natural gas.
  • the molecular weight of the condensate after the cooling step followingthe intermediate compression stage is about 40 to 70, preferably 50 to 60, and that of the resultant vapor about 20 to 40, preferably 20 to 30.
  • the advantage of the abovedescribed system resides in that the refrigeration capacity of the cycle is increased, due to the presence of larger amounts of C -C hydrocarbons, and that simultaneously, by the partial condensation after the intermediate cooling in the intercooler, the partial pressure of these hydrocarbons in the refrigeration medium passing into the lowest temperature stages is maintained at such a low level that there is no undesired increase of th vaporization temperature in such stages.
  • FIG. 1 is a schematic diagram of a preferred embodiment of this invention wherein the natural gas is intermixed with cycle fluid.
  • FIG. 2 is a schematic diagram of another preferred embodiment wherein the natural gas is liquefied independent of any intermixing with cycle fluid.
  • the pressure of the intermediate compression stage and the content of C -C hydrocarbons in the cycle fluid are adjusted.
  • the pressure of the intermediate compression stage is advantageous for the pressure of the intermediate compression stage to be the same or substantially the same as the natural gas pressure, generally about 45 to 35, preferably 10 to 25 atrnospheres absolute.
  • the cycle gas must have about the following composition:
  • the invention is applied in a particularly suitable manner to a process wherein the required refrigeration is produced by a single cycle, and the cycle fluid is subjected to a multi-stage partial condensation, where, in each instance, the condensate is separated, expanded to the inlet pressure of the circulation compressor, vaporized and'warmed in heat exchange with cycle fluid and natural gas, and recycled to the circulation compressor.
  • a high liquefaction efficiency is obtained witha low expenditure in apparatus, and, furthermore, the process can be easily adapted to various natural gas compositions and operating conditions.
  • the apparatus for conducting the process according to the invention comprises as the essential novelty, a separator connected after at least one intercooler of the circulation compressor, which separator is in communication in the gas phase via a conduit, with the subsequent compression stage and, in the liquid phase, via an expansion valve, and the refrigerating cycle path of a heat exchanger, with the inlet side of the circulation compressor, and associated conduit.
  • FIG. 1 shows a process with arropen cycle, i.e. wherein the natural gas to be liquefied is compressed and brought to a low temperature together with the cycle gas.
  • the cycle fluid has approximately the following composition:
  • 20,000 Nm lh of the cycle gas is fed at about 6 atmospheres absolute through conduit 1 to the inletside of the first compressor stage 2, compressed at that point to about 20 atmospheres absolute, and brought to the cooling water temperature in the intercooler 3.
  • 1,000 Nmlh of the cycle fluid are liquefied during this step, separated from the gaseous phase in the separator 4, cooled to about 280K. in, the heat exchanger 5, and expanded through valve 6 into the conduit 1 whereupon it is then reintroduced to the first stage of the compressor.
  • the gas leaving the separator 4, together with 6,000 Nm /h of natural gas (freed of C0,, H 8, and B 0), is compressed in the second compressor stage 8 to about 35 atmospheres absolute.
  • the final cooler 9 there is again obtained about 1,000 Nm /h of liquid, the
  • a small portion of the subcooled liquid from separator 10 is expanded, at the. cold" end of the heat exchanger 5, via valve 13 into the conduit 27 leading to the gasometer.
  • the amount and composition of this stream are chosen so that the C,- and higher hydrocarbons entering the plant together with the natural gas again are discharged from the plant by this path.
  • the gas from the separator 10 is cooled, in heat exchanger 5, to about 280K. and is partially coridensed during this step.
  • the liquid about 4,200 Nm lh, is separated from the vapor. Both fractions are cooled in heat exchanger 15 to about 245K.
  • the subcooled liquid is expanded, admixed 'to the returning cycle gas, and vaporized in heat exchanger l5.
  • the gas is once again partially condensed and separated, in separator 16, into a liquid and a gaseous phase.
  • the amount of the thus-formed liquid is about 6,000 Nm /h.
  • the .vapor separated in separator 20 is cooled, liquefied, and subcooled in heat exchangers 21 and 23.
  • the liquid passes at a temperature of about 115K. into the storage tank 25 by way of expansion valve 24.
  • the temperature at the cold end of the heat exchanger 23 is obtained by expansion and vaporization of a portion of the liquid leaving the heat exchanger 23; this liquidis expanded via valve 26 into the conduit 27 leading to the gasometer, and is discharged from the plant via the heat exchangers 23, 21, 19, 17, 15, and 5.
  • the gas vaporized in the storage tank 25 by the effect of heat is withdrawn via conduit 28 and conveyed, through the cold gas blower 29, and via conduit 27 to the gasometer.
  • the pressure and temperature conditions ambient in the individual separators are set forth (P in atmospheres absolute, Tin K.), as well as the total amount fed to each separator (F in Nm lh), the amount of liquid separated therein (1. in Nm lh), and also the approximate molecular weight of the it can be seen from the above table that in the separator 4, propane (molecular weight 44) and the higher hydrocarbons are obtained in the liquid phase.
  • the liquid in separator consists essentially of propane; in separators l4 and 16, the proportion of ethane (molecular weight 30) increases in the liquid.
  • separators 18 and 20 a mixture of ethane and methane (molecular weight 16) is separated.
  • the gas leaving the separator 20 is mostly methane.
  • the molecular weight of the gaseous phase decreases from separator to separator.
  • the cycle fluid has the following compositions:
  • the improvement comprising employing as said circulation compressor, a multi-stage compressor, adjusting the concentration of C,,- to C,- hydrocarbons in the cycle fluid, and the pressure of at least one intermediate stage of the circulation compressor, with respect to each other so that a portion of the effluent from said intermediate stage is condensible by heat exchange with cooling water; cooling said effluent from said intermediate stage in an intercooler between two successive pressure stages to form a liquid phase condensate containing a substantial concentration of heavy hydrocarbons and a vapor phase; separating said condensate from said vapor phase; pressure-reducing said condensate exclusively of any condensate of said vapor phase separated therefrom; vaporizing and heating resultant pressure-reduced condensate in heat exchange with the natural gas to be liquefied and the cycle fluid; recycling resultant heated vaporized condensate to the inlet side of the circulation compressor, recompressing said vapor separated from said condensate containing a substantial concentration of heavy hydrocarbons, and subject
  • said natural gas being intermixed with cycle fluid.
  • Apparatusifor the liquefaction of natural gas comprising:
  • a condensate separator (4) having inlet means and gas outlet means and liquid outlet means;
  • At least one intercooler (3) having inlet and outlet means; said inlet means of said condensate separator being in communication with said outlet means of said intercooler;
  • a circulation compressor having at least two serially connected compression stages, said inlet means of said intercooler being in communication with the outlet of an intermediate compression stage, said gas outlet means of said condensate separator being disposed before, and in communication with the inlet side of the last serially connected compression stage ⁇ (8);
  • an expansion valve (6) being in communication with the liquid outlet means of said condensate separator and separate unbranched conduit means for conducting liquid from said liquid outlet means exclusively to said expansion valve;
  • heat exchange means includingseparate flow paths for expanded condensate, natural gas to be liquefied, and cycle liquid; and conduit means for effecting said communications and also for recirculating resultant heated expanded condensate from said heatexchange' means and said expansion valve to the inlet of said circulation compressor, and
  • liquid phase condensate having a substantial concentration of heavy hydrocarbons having a molecular weight of about -70 and said vapor phase separated therefrom having a molecular weight of about 20-40.
  • liquid phase condensate having a substantial concentration of heavy hydrocarbons having a molecular weight of about -60 and said vapor phase separated therefrom having a molecularlweight of about 20-30.
  • a process as defined b claim 2 comprising the steps of passing said vapor separated from said condensate having a substantial concentration of heavy hydrocarbons to a final compression stage of said multi-stage compressor; cooling resultant compressed vapor to form a liquid phase and a vapor phase; passing the just-mentioned liquid phase 7 through a heat exchanger, and expanding a portion of resultant heat exchanged fluid and discharging the latter from said liquefaction cycle, said portion being of sufficient amount and of a composition to remove C and higher hydrocarbons from the natural gas intermixed with said cycle fluid.

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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)
US873964A 1968-11-04 1969-11-04 Refrigeration cycle for the aliquefaction of natural gas Expired - Lifetime US3702063A (en)

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DE19681806879 DE1806879C3 (de) 1968-11-04 Verfahren zum Verflüssigen von Erdgas

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US3702063A true US3702063A (en) 1972-11-07

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JP (1) JPS5440512B1 (fr)
FR (1) FR2022550B1 (fr)
GB (1) GB1278974A (fr)

Cited By (22)

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Publication number Priority date Publication date Assignee Title
US3874184A (en) * 1973-05-24 1975-04-01 Phillips Petroleum Co Removing nitrogen from and subsequently liquefying natural gas stream
US3879180A (en) * 1971-12-18 1975-04-22 Gutehoffnungshuette Sterkrade Method for treating a gas current which is obtained by coal gasification
US3884044A (en) * 1970-02-09 1975-05-20 Exxon Research Engineering Co Mixed refrigerant cycle
US3884045A (en) * 1970-02-09 1975-05-20 Exxon Research Engineering Co Mixed refrigerant cycle
US3914949A (en) * 1971-02-19 1975-10-28 Chicago Bridge & Iron Co Method and apparatus for liquefying gases
US3945214A (en) * 1973-07-03 1976-03-23 Societe Des Procedes L'air Liquide Et Technip De Liquefaction Des Gaz Naturels Method and apparatus for cooling a gas
US4303427A (en) * 1976-06-23 1981-12-01 Heinrich Krieger Cascade multicomponent cooling method for liquefying natural gas
US4325231A (en) * 1976-06-23 1982-04-20 Heinrich Krieger Cascade cooling arrangement
US4707170A (en) * 1986-07-23 1987-11-17 Air Products And Chemicals, Inc. Staged multicomponent refrigerant cycle for a process for recovery of C+ hydrocarbons
US6751984B2 (en) * 2000-02-10 2004-06-22 Sinvent As Method and device for small scale liquefaction of a product gas
US20070283718A1 (en) * 2006-06-08 2007-12-13 Hulsey Kevin H Lng system with optimized heat exchanger configuration
US20090095019A1 (en) * 2006-05-15 2009-04-16 Marco Dick Jager Method and apparatus for liquefying a hydrocarbon stream
FR2944096A1 (fr) * 2009-04-07 2010-10-08 Ass Pour La Rech Et Le Dev De Procede et systeme frigorifique pour la recuperation de la froideur du methane par des fluides frigorigenes.
WO2010128467A2 (fr) * 2009-05-08 2010-11-11 Corac Group Plc Production et distribution de gaz naturel
CN102564057A (zh) * 2011-12-19 2012-07-11 中国海洋石油总公司 一种应用于基荷型天然气液化工厂的丙烷预冷混合冷剂液化系统
CN102654346A (zh) * 2012-05-22 2012-09-05 中国海洋石油总公司 一种丙烷预冷双混合冷剂并联液化系统
US20120227418A1 (en) * 2011-03-08 2012-09-13 Linde Aktiengesellschaft Cooling unit
EP3252408A1 (fr) * 2016-06-02 2017-12-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de purification de gaz naturel et de liquéfaction de dioxyde de carbone
US10539363B2 (en) 2008-02-14 2020-01-21 Shell Oil Company Method and apparatus for cooling a hydrocarbon stream
EP3368630B1 (fr) 2015-10-27 2020-12-02 Linde GmbH Réfrigérant mélangé basse température pour pré-refroidissement d'hydrogène à grande échelle
US11060037B2 (en) 2015-07-23 2021-07-13 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method for purifying a gas rich in hydrocarbons
EP4450909A1 (fr) * 2023-04-21 2024-10-23 Cryocollect Procédé de liquéfaction d'un gaz

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Publication number Priority date Publication date Assignee Title
MY122625A (en) * 1999-12-17 2006-04-29 Exxonmobil Upstream Res Co Process for making pressurized liquefied natural gas from pressured natural gas using expansion cooling

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GB895094A (en) * 1959-10-21 1962-05-02 Shell Int Research Improvements in or relating to process and apparatus for liquefying natural gas
US3274787A (en) * 1961-06-01 1966-09-27 Air Liquide Method for cooling a gaseous mixture to a low temperature
US3364685A (en) * 1965-03-31 1968-01-23 Cie Francaise D Etudes Et De C Method and apparatus for the cooling and low temperature liquefaction of gaseous mixtures
FR1557019A (fr) * 1965-06-29 1969-02-14
US3548606A (en) * 1968-07-08 1970-12-22 Phillips Petroleum Co Serial incremental refrigerant expansion for gas liquefaction

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Cited By (32)

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US3884044A (en) * 1970-02-09 1975-05-20 Exxon Research Engineering Co Mixed refrigerant cycle
US3884045A (en) * 1970-02-09 1975-05-20 Exxon Research Engineering Co Mixed refrigerant cycle
US3914949A (en) * 1971-02-19 1975-10-28 Chicago Bridge & Iron Co Method and apparatus for liquefying gases
US3879180A (en) * 1971-12-18 1975-04-22 Gutehoffnungshuette Sterkrade Method for treating a gas current which is obtained by coal gasification
US3874184A (en) * 1973-05-24 1975-04-01 Phillips Petroleum Co Removing nitrogen from and subsequently liquefying natural gas stream
US3945214A (en) * 1973-07-03 1976-03-23 Societe Des Procedes L'air Liquide Et Technip De Liquefaction Des Gaz Naturels Method and apparatus for cooling a gas
US4303427A (en) * 1976-06-23 1981-12-01 Heinrich Krieger Cascade multicomponent cooling method for liquefying natural gas
US4325231A (en) * 1976-06-23 1982-04-20 Heinrich Krieger Cascade cooling arrangement
US4707170A (en) * 1986-07-23 1987-11-17 Air Products And Chemicals, Inc. Staged multicomponent refrigerant cycle for a process for recovery of C+ hydrocarbons
US6751984B2 (en) * 2000-02-10 2004-06-22 Sinvent As Method and device for small scale liquefaction of a product gas
US20090095019A1 (en) * 2006-05-15 2009-04-16 Marco Dick Jager Method and apparatus for liquefying a hydrocarbon stream
US8578734B2 (en) * 2006-05-15 2013-11-12 Shell Oil Company Method and apparatus for liquefying a hydrocarbon stream
US20070283718A1 (en) * 2006-06-08 2007-12-13 Hulsey Kevin H Lng system with optimized heat exchanger configuration
US10539363B2 (en) 2008-02-14 2020-01-21 Shell Oil Company Method and apparatus for cooling a hydrocarbon stream
AU2010233573B2 (en) * 2009-04-07 2016-10-27 Association Pour La Recherche Et Le Developpement De Methodes Et Processus Industriels "Armines" Refrigeration process and system for recovering cold from methane by refrigerants
FR2944096A1 (fr) * 2009-04-07 2010-10-08 Ass Pour La Rech Et Le Dev De Procede et systeme frigorifique pour la recuperation de la froideur du methane par des fluides frigorigenes.
CN102414528A (zh) * 2009-04-07 2012-04-11 工业加工方法研究和发展协会“阿美尼斯” 用于从甲烷致冷剂回收冷量的致冷方法和系统
WO2010116067A3 (fr) * 2009-04-07 2011-11-10 Association Pour La Recherche Et Le Developpement De Methodes Et Processus Industriels "Armines" Procede et systeme frigorifique pour la recuperation de la froideur du methane par des fluides frigorigenes
CN102414528B (zh) * 2009-04-07 2014-03-19 工业加工方法研究和发展协会“阿美尼斯” 用于从甲烷致冷剂回收冷量的致冷方法和系统
US8826677B2 (en) 2009-04-07 2014-09-09 Association Pour la Recherche et le Developpement de Methodes et Processus Industriels “Armines” Refrigeration process and system for recovering cold from methane by refrigerants
WO2010116067A2 (fr) * 2009-04-07 2010-10-14 Association Pour La Recherche Et Le Developpement De Methodes Et Processus Industriels "Armines" Procede et systeme frigorifique pour la recuperation de la froideur du methane par des fluides frigorigenes
WO2010128467A3 (fr) * 2009-05-08 2011-12-29 Corac Group Plc Production et distribution de gaz naturel
WO2010128467A2 (fr) * 2009-05-08 2010-11-11 Corac Group Plc Production et distribution de gaz naturel
US20120227418A1 (en) * 2011-03-08 2012-09-13 Linde Aktiengesellschaft Cooling unit
CN102564057A (zh) * 2011-12-19 2012-07-11 中国海洋石油总公司 一种应用于基荷型天然气液化工厂的丙烷预冷混合冷剂液化系统
CN102654346A (zh) * 2012-05-22 2012-09-05 中国海洋石油总公司 一种丙烷预冷双混合冷剂并联液化系统
US11060037B2 (en) 2015-07-23 2021-07-13 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method for purifying a gas rich in hydrocarbons
EP3368630B1 (fr) 2015-10-27 2020-12-02 Linde GmbH Réfrigérant mélangé basse température pour pré-refroidissement d'hydrogène à grande échelle
FR3052241A1 (fr) * 2016-06-02 2017-12-08 L'air Liquide Sa Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de purification de gaz naturel et de liquefaction de dioxyde de carbone
US10415879B2 (en) 2016-06-02 2019-09-17 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process for purifying natural gas and liquefying carbon dioxide
EP3252408A1 (fr) * 2016-06-02 2017-12-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de purification de gaz naturel et de liquéfaction de dioxyde de carbone
EP4450909A1 (fr) * 2023-04-21 2024-10-23 Cryocollect Procédé de liquéfaction d'un gaz

Also Published As

Publication number Publication date
FR2022550A1 (fr) 1970-07-31
GB1278974A (en) 1972-06-21
FR2022550B1 (fr) 1973-12-07
DE1806879A1 (de) 1970-05-27
JPS5440512B1 (fr) 1979-12-04
DE1806879B2 (de) 1975-10-30

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