US3874185A - Process for a more efficient liquefaction of a low-boiling gaseous mixture by closely matching the refrigerant warming curve to the gaseous mixture cooling curve - Google Patents

Process for a more efficient liquefaction of a low-boiling gaseous mixture by closely matching the refrigerant warming curve to the gaseous mixture cooling curve Download PDF

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US3874185A
US3874185A US393331A US39333173A US3874185A US 3874185 A US3874185 A US 3874185A US 393331 A US393331 A US 393331A US 39333173 A US39333173 A US 39333173A US 3874185 A US3874185 A US 3874185A
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fraction
cycle
gaseous mixture
nitrogen
natural gas
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Volker Etzbach
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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
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
    • 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
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • 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
    • F25J1/0204—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 as a single flow SCR 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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • 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
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • 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
    • F25J1/0277—Offshore use, e.g. during shipping
    • 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.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • This simple process has the disadvantage that the isentropically expanded cycle fraction transmits its peak cold essentially at a constant temperature, but the natural gas to be liquefied, due to the nitrogen enrichment, can absorb the peak cold only at a falling temperature.
  • the refrigeration is available in the conventional process at a lower temperature level than is required for actual cooling purposes, so that necessarily larger temperature differences occur in the heat exchangers, thereby increasing the energy requirements of the system.
  • the invention is directed to the problem of developing a simple and energy-conserving process for the liquefaction of low-boiling gaseous mixtures.
  • the abovedescribed problem is solved by a process wherein the peak cold required for the liquefaction of the gaseous mixture is provided by warming an isentropically expanded partial stream of the cycle gas and the residual cold is provided by vaporization of the residual stream of the cycle gas which has been at least partially condensed by isenthalpic expansion.
  • the cooling curves of low-boiling gaseous mixtures are relatively flat, with a small dQ/dT in the low-temperature range, i.e., in the range of the peak cold, i.e., the lowest portion of its liquefaction zone, when the proportion of the lower-boiling component is relatively small compared to the other components, whereas in the zone of higher temperatures, the dQ/dT first increases markedly dut to vaporization of the main component, and then decreases again due to gas warming.
  • This adaptation is maximally provided by the process of the present invention by employing, for producing the peak cold i.e., the lowest temperatures of the gaseous mixture, an isentropically expanded first fraction of the cycle gas which, after the expansion, is entirely in the gaseous phase, i.e., which is not expanded into the liquid-vapor region.
  • the warming-up curve of such a gaseous fraction has only a minor dQ/dT in the low temperature zones at which the heat exchange with the gaseous mixture takes place.
  • the heat exchange is effected with an isenthalpically expanded residual second fraction of the cycle gas, the pressure of which can be higher than the final pressure resulting from the isentropic expansion.
  • the equipment for performing the process of this invention is constructionally particularly simple, the process is especially well suitable for the reliquefaction of evaporated nitrogen-containing natural gas in tanker ships.
  • the cold production by the process can be simply and readily adapted to the resulting fluctuating cold requirements in accordance with a preferred embodiment of this invention, by subjecting the residual second fraction to a bar phase separation after its isenthalpic expansion but prior to heat exchange.
  • a portion of the liquid fraction obtained by this phase separation is stored instead of being conveyed to the heat exchange zone and, during periods of highest refrigeration requirements, at least a portion of the thus-stored liquid fraction of the cycle gas is again fed into the cycle to the heat exchange zone.
  • the amount of the gaseous mixture fed to the liquefaction stage per unit of time is reduced and a part of the liquid fraction obtained during the phase separation is then stored.
  • the amount of circulated cycle gas is decreased and, consequently, the cycle compressor achieves a correspondingly lower compression of the cycle gas, so that the total refrigeration output of the cycle is reduced.
  • the phase separation takes place in a separator, the latter itself and/or a separate storage tank can be utilized.
  • the cold gaseous fraction ofthe cycle gas obtained during the phase separation is again amixed with the portion of the condensed fraction utilized for the heat exchange with the gaseous mixture to be liquefied, directly after the complete evaporation of this condensed fraction, so that the refrigeration capability of the gaseous fraction produced during the phase separation can also be made available to the system.
  • the energy liberated during the isentropic expansion of the partial fraction of the cyclegas can conventionally be utilized for the compression of the cycle gas.
  • FIG. 1 is a schematic flow sheet of an embodiment of the process of this invention
  • FIG. 2 is a graphic representation of the cooling and warming curves, respectively, based on the embodiment of FIG. 1;
  • FIG. 3 is a schematic illustration of another embodiment of the process of this invention.
  • natural gas to be liquefied is withdrawn via conduit 1 from a storage tank 2 by a blower l5, liquefied in heat exchange with cycle gas in heat exchangers 3 and 4, and recycled into storage tank 2.
  • the portion of the natural gas which cannot be liquefied or can be liquefied only with great difficulty, i.e., at very low temperatures, is separated in separator 16 and either combusted in a steam boiler or exhausted into the atmosphere.
  • the refrigeration required for liquefying the natural gas is produced by a closed nitrogen cycle wherein nitrogen is compressed in compressors 5 and 6 and in a high-pressure compression blower 7 to the required cycle pressure of about 45 atmospheres absolute. Water coolers 8, 9, and 10, respectively, are connected after each compression stage.
  • first heat exchanger 11 the compressed nitrogen is cooled in heat exchange with colder nitrogen to about 166 K and then divided into two first and second fractions.
  • the first fraction is expanded isentropically in the turbine 12 to about 4.5 atm. abs. and fed at the resultant temperature of about 93 K to the heat exchanger 4, wherein this fraction is warmed to about 105 K by heat exchange with the natural gas while giving up the peak cold required for the liquefaction of the natural gas.
  • the fraction then flows at this temperature to a heat exchanger 13, where it is warmed by heat exchange with the second residual fraction, to about 146 K.
  • the second residual fraction is partially liquefied in this step.
  • the first fraction then flows to heat exchanger 1 1 where it provides the colder nitrogen and, after further warming in heat exchanger 11, the first fraction is fed to the inlet of the low-pressure compressor 5 and, after passing through heat exchanger 8, is introduced into the inlet of intermediate-pressure compressor 6.
  • the second residual fraction is partially liquefied in heat exchanger 13 and is isenthalpically expanded in a throttle valve 14 to about 10 atm. abs. and is then fed to heat exchanger 3 at a temperature of about 103 K, wherein it is vaporized by heat exchange with the natural gas and warmed to about 146 K.
  • This second residual fraction then flows through heat exchanger 11 with further warming and is then introduced into the inlet of intermediate-pressure compressor 6, where it is further compressed as a mixture with the first fraction.
  • FIG. 2 shows the course of the cooling and warming curves in heat exchangers 3 and 4, wherein the heat exchange zone of heat exchanger 3 is indicated by A and the zone heat exchange of heat exchanger 4 is denoted by B.
  • FIG. 3 shows another embodiment of the process of this invention which makes it possible to adapt the cold production of the cycle to a gaseous mixture to be liquefied which is available in varying amounts per unit time.
  • the gas which evaporates from liquid, nitrogen-containing natural gas in storage tank 20 is withdrawn via conduit 21 and compressed to about 1.3 atm. abs. by a blower 22, at least partially liquefied in heat exchanger 24 in heat exchange with a isenthalpically and isentropically expanded cycle gas, and then fed to a separator 25, where a partial fraction, enriched in nitrogen and not liquefied during this heat exchange at an adjustable low temperature of, for example, K, is withdrawn via conduit 26, and vented or used, for example as fuel gas, while the residual liquid fraction is recycled to storage tank 20 via conduit 27.
  • the refrigeration required for the liquefaction of the volatilized natural gas is produced in a closed nitrogen cycle, wherein nitrogen is compressed in compressors 28 and 29, as well as in compression blower 30, to the cycle pressure of about 45 atm. abs. required during normal operation.
  • these three compressors are associated with water coolers 31, 32, and 33, respectively.
  • the compressed nitrogen is further cooled in heat exchange with itself to about 167 K and then divided into first and second streams.
  • the first stream is isentropically expanded to about 4.5 atm. abs. by turbine 35 and then fed at the temperature of about 93 K resulting from the expansion to the heat exchanger 24, wherein it is warmed by heat exchange with the natural gas to about 103 K while providing the peak cold, i.e., lowest heat exchange temperature, required for the liquefaction of the gaseous natural gas.
  • the second stream of nitrogen after being cooled in heat exchanger 36 by heat exchange with the first stream of nitrogen, is expanded in throttle valve 37 to about atm. abs. and thereafter subjected to a phase separation in separator 38.
  • the liquid portion obtained by the phase separation of the second stream is completely withdrawn via conduit 39, in normal operation, and fed to the upper section ofthe heat exchanger 24 at a temperature of about 103 K, wherein it is first completely vaporized by heat exchange with the natural gas and then combined with the gaseous portion of the second stream obtained in separator 38, and withdrawn therefrom via conduit 40.
  • the resulting mixture is warmed to ambient temperature in heat exchanger 34 and finally fed to the inlet of the intermediate-pressure compressor 29, where it is further compressed as a mixture with the first stream.
  • liquid nitrogen stored in separator 38 is fed into the cycle by opening wider valve 41.
  • additional refrigeration in the form ofliquid nitrogen is made immediately available to the refrigeration cycle, and, as a result of the increased amount of cycle gas being circulated, a higher compression ofthe cycle gas is achieved in the cycle compressors, thereby increasing the total refrigeration capacity of the system.
  • gaseous mixture is nitrogen-containing natural gas volatilized from stored liquid natural gas, and the cycle gas is nitrogen.
  • gaseous mixture is nitrogen-containing natural gas volatil-. ized from stored liquid natural gas, and the cycle gas is nitrogen.
  • gaseous mixture is nitrogen-containing natural gas volatilized from stored liquid natural gas
  • cycle gas is

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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)
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  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US393331A 1972-12-18 1973-08-31 Process for a more efficient liquefaction of a low-boiling gaseous mixture by closely matching the refrigerant warming curve to the gaseous mixture cooling curve Expired - Lifetime US3874185A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE2261886A DE2261886C3 (de) 1972-12-18 1972-12-18 Verfahren zum Verflüssigen von^^,,^,, Gasgemischen
DE2319803A DE2319803C3 (de) 1973-04-18 1973-04-18 Verfahren zum Verflüssigen von tiefsiedenden Gasgemischen

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US (1) US3874185A (ko)
JP (1) JPS5632539B2 (ko)
FR (1) FR2210752B1 (ko)
GB (1) GB1395270A (ko)
IT (1) IT1002519B (ko)
NL (1) NL7315311A (ko)
NO (1) NO133287C (ko)
SE (1) SE395315B (ko)

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4727723A (en) * 1987-06-24 1988-03-01 The M. W. Kellogg Company Method for sub-cooling a normally gaseous hydrocarbon mixture
US4758257A (en) * 1986-05-02 1988-07-19 The Boc Group Plc Gas liquefaction method and apparatus
US4843829A (en) * 1988-11-03 1989-07-04 Air Products And Chemicals, Inc. Reliquefaction of boil-off from liquefied natural gas
US4846862A (en) * 1988-09-06 1989-07-11 Air Products And Chemicals, Inc. Reliquefaction of boil-off from liquefied natural gas
WO1994013376A1 (en) 1992-12-07 1994-06-23 Edwards Engineering Corp. Vapor recovery apparatus and method
US5483806A (en) * 1994-05-16 1996-01-16 Miller; Jeremy P. Refrigeration system
EP0763848A2 (en) * 1995-09-15 1997-03-19 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Refrigeration system and method for cooling a susceptor using a refrigeration system
WO2000025061A1 (en) * 1998-10-23 2000-05-04 Exxonmobil Upstream Research Company Reliquefaction of boil-off from pressure lng
EP1120615A2 (en) * 2000-01-26 2001-08-01 Cryostar-France SA Apparatus for reliquefying compressed vapour
US6449983B2 (en) 2000-03-09 2002-09-17 The Boc Group, Inc. Reliquefaction of compressed vapor
KR100356764B1 (ko) * 1997-03-21 2002-10-18 크배르너 마리타임 에이.에스 액화 천연가스의 보관 및 운송을 위한 방법 및 장치
US6619047B2 (en) * 2001-06-20 2003-09-16 Linde Aktiengesellschaft Method and device for a cooling system
US6672104B2 (en) 2002-03-28 2004-01-06 Exxonmobil Upstream Research Company Reliquefaction of boil-off from liquefied natural gas
WO2005071333A1 (en) * 2004-01-23 2005-08-04 Hamworthy Kse Gas Systems As Method for re-liquefaction of boil-off gas
KR100699163B1 (ko) 2005-11-17 2007-03-23 신영중공업주식회사 Ｌｎｇ ｂｏｇ의 재액화 장치 및 재액화 방법
EP1860393A1 (en) * 2006-05-23 2007-11-28 Cryostar SAS Method and apparatus for the reliquefaction of a vapour
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EP2229567A4 (en) * 2007-12-06 2018-01-24 Aragon AS Method and system for regulation of cooling capacity of a cooling system based on a gas expansion process.
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FR3087524A1 (fr) 2018-10-22 2020-04-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et une installation de liquefaction de gaz naturel
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KR100699163B1 (ko) 2005-11-17 2007-03-23 신영중공업주식회사 Ｌｎｇ ｂｏｇ의 재액화 장치 및 재액화 방법
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WO2008022689A2 (de) * 2006-08-25 2008-02-28 Linde Aktiengesellschaft Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes
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US20080190117A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and operation of the same
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US20080190118A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and unloading of lng from the tank
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US8028724B2 (en) 2007-02-12 2011-10-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and unloading of LNG from the tank
US20090266086A1 (en) * 2007-04-30 2009-10-29 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Floating marine structure having lng circulating device
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
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US7841288B2 (en) 2008-02-11 2010-11-30 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
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US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
WO2010104498A1 (en) * 2009-01-14 2010-09-16 Mustang Engineering, L.P. Methods and apparatus for liquefaction of natural gas and products therefrom
CN101852534A (zh) * 2009-03-31 2010-10-06 林德股份公司 用于使富含烃类的馏份液化的方法
CN101886006A (zh) * 2009-05-12 2010-11-17 林德股份公司 用于液化富烃馏分的方法
US11153991B2 (en) * 2017-02-08 2021-10-19 Linde Aktiengesellschaft Method and apparatus for cooling a load and system comprising corresponding apparatus and load
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US10704830B2 (en) 2018-01-24 2020-07-07 Gas Technology Development Pte Ltd Process and system for reliquefying boil-off gas (BOG)
FR3087524A1 (fr) 2018-10-22 2020-04-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et une installation de liquefaction de gaz naturel
FR3087525A1 (fr) 2018-10-22 2020-04-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de liquefaction d'un courant gazeux d'evaporation issu du stockage d'un courant de gaz naturel liquefie

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JPS4990277A (ko) 1974-08-28
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NO133287B (ko) 1975-12-29
SE395315B (sv) 1977-08-08
GB1395270A (en) 1975-05-21
FR2210752B1 (ko) 1977-06-10
JPS5632539B2 (ko) 1981-07-28
NL7315311A (ko) 1974-06-20
NO133287C (ko) 1976-04-07

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