US20100115990A1 - Method for liquefying a hydrocarbon-rich flow - Google Patents

Method for liquefying a hydrocarbon-rich flow Download PDF

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Publication number
US20100115990A1
US20100115990A1 US12/438,500 US43850007A US2010115990A1 US 20100115990 A1 US20100115990 A1 US 20100115990A1 US 43850007 A US43850007 A US 43850007A US 2010115990 A1 US2010115990 A1 US 2010115990A1
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United States
Prior art keywords
refrigerant mixture
vaporising
separated
incomplete
fractions
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Abandoned
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US12/438,500
Inventor
Wolfgang Förg
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Shell USA Inc
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Individual
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Filing date
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Assigned to SHELL OIL COMPANY reassignment SHELL OIL COMPANY ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FORG, WOLFGANG
Publication of US20100115990A1 publication Critical patent/US20100115990A1/en
Abandoned 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
    • F25J1/003—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
    • F25J1/0002—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
    • 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
    • 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
    • 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
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
    • 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.
    • F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
    • 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

Definitions

  • the invention relates to a method for liquefying a hydrocarbon-rich flow, in particular a natural gas flow, via indirect heat exchange with the refrigerant mixture of a refrigerant mixture circuit.
  • Such methods for liquefying a hydrocarbon-rich flow are generally designated as “Single-Flow Mixed Refrigerant Cycle”.
  • a common element here is that the refrigerant mixture is fully vaporised prior to (again) being fed to the circuit compressor and is superheated by ca, 10 K above its dew point.
  • the aim of the present invention is to provide a generic method for liquefying a hydrocarbon-rich flow, by which the abovementioned considerable disadvantage can be avoided.
  • a generic method for liquefying a hydrocarbon-rich flow whereby the refrigerant mixture is compressed two-stage or multistage, is separated into at least one lower-boiling and at least one higher-boiling refrigerant mixture fraction and the refrigerant mixture fractions are vaporised at different temperature levels against the hydrocarbon-rich flow to be cooled and liquefied, and then unified prior to recompression, and whereby the refrigerant mixture fractions are not fully vaporised.
  • the refrigerant mixture fractions are not superheated, in particular they are not superheated above their dew point, and more particularly are not superheated by ca. 10 K above their dew point.
  • the quantity of liquid or fraction resp. resulting from incomplete vaporising of the refrigerant mixture prior to feeding the refrigerant mixture to the circuit compressor is preferably separated off, since it can otherwise result in damage to the circuit compressor. It is also possible to provide at least one extra pump, by means of which the separated quantity of liquid or fraction resp. can be pumped to a suitable site inside the refrigerant mixture circuit. Referring for example to FIG. 1 of the abovementioned German patent 197 22 490, the quantity of liquid or fraction resp. accruing in a separator D 2 upstream of the compressor V is fed to the separator D 3 , preferably using a pump.
  • thermodynamic advantage Apart from the advantage of safe operation, which is associated with the method according to the invention for liquefying a hydrocarbon-rich flow, a not inconsiderable thermodynamic advantage can also be realised, Due to so-called “wet operation”, i.e. non-attainment of the dew point inside the heat exchanger, the sharp knee at the dew point in the enthalpy temperature diagram of the refrigerant mixture is also avoided. The result of this is that the heating and cooling curves can be better matched, again resulting in an improvement in efficiency of the overall process.
  • the method can also be employed to advantage in other refrigerant mixture methods for liquefying hydrocarbon-rich flow, in addition to the “Single-Flow Mixed Refrigerant Cycle method”.

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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)
  • Agricultural Chemicals And Associated Chemicals (AREA)

Abstract

Disclosed is a method for liquefying a hydrocarbon-rich stream, in particular a natural gas stream, by indirectly exchanging hear with the coolant mixture of a coolant mixture circuit. In said method, the coolant mixture is condensed in two or more stages, is divided into at least one lower-boiling and at least one higher-boiling coolant mixture fraction, and the coolant mixture fractions are evaporated at different temperature levels against the hydrocarbon-rich stream that is to be cooled and liquefied and are then combined before being condensed once again. The coolant mixture fractions are not entirely evaporated during normal operation and are preferably not superheated. Preferably, at least 1 to 10 percent by weight of the total amount of the coolant mixture are not evaporated.

Description

  • The invention relates to a method for liquefying a hydrocarbon-rich flow, in particular a natural gas flow, via indirect heat exchange with the refrigerant mixture of a refrigerant mixture circuit.
  • A generic method for liquefying a hydrocarbon-rich flow is known for example from German patent 197 22 490. By citing this document the disclosure thereof shall be incorporated into the disclosure of the present patent application in its entirety.
  • Such methods for liquefying a hydrocarbon-rich flow, as described in the abovementioned patent, are generally designated as “Single-Flow Mixed Refrigerant Cycle”. A common element here is that the refrigerant mixture is fully vaporised prior to (again) being fed to the circuit compressor and is superheated by ca, 10 K above its dew point.
  • In the operating of generic methods for liquefying a hydrocarbon-rich flow it has been shown however that this heating of the refrigerant mixture over and above the dew point can be highly problematic, since thermal fluctuations arise in the region of the dew point, which can cause breakages in the pipes of lapped heat exchangers, preferably in the outer pipe layers. The consequence of such pipe breakage is generally unwanted interruption of the liquefaction process.
  • Other generic methods for liquefying a hydrocarbon-rich flow are for example the so-called “Parallel Mixed Refrigerant” method, as described for example in U.S. Pat. No. 6,389,844; the so-called “Double Mixed Refrigerant” method, such as described for example in U.S. Pat. No. 6,370,910; or other refrigerant mixture methods with pre-cooling circuit, such as for example a “Propane-Mixed Refrigerant” method.
  • The aim of the present invention is to provide a generic method for liquefying a hydrocarbon-rich flow, by which the abovementioned considerable disadvantage can be avoided.
  • To solve this problem a generic method for liquefying a hydrocarbon-rich flow is proposed, whereby the refrigerant mixture is compressed two-stage or multistage, is separated into at least one lower-boiling and at least one higher-boiling refrigerant mixture fraction and the refrigerant mixture fractions are vaporised at different temperature levels against the hydrocarbon-rich flow to be cooled and liquefied, and then unified prior to recompression, and whereby the refrigerant mixture fractions are not fully vaporised.
  • A further advantageous accomplishment is that the refrigerant mixture fractions are not superheated, in particular they are not superheated above their dew point, and more particularly are not superheated by ca. 10 K above their dew point.
  • In further advantageous configurations of the method according to the invention for liquefying a hydrocarbon-rich flow, which constitute the subject matter of the dependent claims, it is proposed that independently or in combination
      • at least 1 to 10% by weight, preferably at least 2 to 5 by weight of the total quantity of the refrigerant mixture is not vaporised;
      • incomplete vaporising of the refrigerant mixture is achieved by the refrigerant mixture having a sufficiently large proportion of heavier hydrocarbons, preferably C4H10— and C5H12— hydrocarbons, depending on the selected method parameters, such as vaporising temperature and pressure;
      • the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated off; and
      • this separated liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit, preferably by means of a pump.
  • In contrast to the previously used methods from now on uninterruptedly in normal operation there is no complete vaporising of the refrigerant mixture and its superheating above the dew point.
  • The quantity of liquid or fraction resp. resulting from incomplete vaporising of the refrigerant mixture prior to feeding the refrigerant mixture to the circuit compressor is preferably separated off, since it can otherwise result in damage to the circuit compressor. It is also possible to provide at least one extra pump, by means of which the separated quantity of liquid or fraction resp. can be pumped to a suitable site inside the refrigerant mixture circuit. Referring for example to FIG. 1 of the abovementioned German patent 197 22 490, the quantity of liquid or fraction resp. accruing in a separator D2 upstream of the compressor V is fed to the separator D3, preferably using a pump.
  • Apart from the advantage of safe operation, which is associated with the method according to the invention for liquefying a hydrocarbon-rich flow, a not inconsiderable thermodynamic advantage can also be realised, Due to so-called “wet operation”, i.e. non-attainment of the dew point inside the heat exchanger, the sharp knee at the dew point in the enthalpy temperature diagram of the refrigerant mixture is also avoided. The result of this is that the heating and cooling curves can be better matched, again resulting in an improvement in efficiency of the overall process.
  • The method can also be employed to advantage in other refrigerant mixture methods for liquefying hydrocarbon-rich flow, in addition to the “Single-Flow Mixed Refrigerant Cycle method”.

Claims (20)

1. A method for liquefying a hydrocarbon-rich flow through indirect heat exchange with the refrigerant mixture of a refrigerant mixture circuit, whereby the refrigerant mixture is compressed two-stage or multistage, is separated into at least one lower-boiling and at least one higher-boiling refrigerant mixture fraction and the refrigerant mixture fractions are vaporised at different temperature levels against the hydrocarbon-rich flow to be cooled and liquefied and are then unified prior to recompression, and whereby the refrigerant mixture fractions are not fully vaporised.
2. A method according to claim 1, whereby at least 1 to 10% by weight of the total quantity of the refrigerant mixture is not vaporised.
3. A method according to claim 1, whereby incomplete vaporising of the refrigerant mixture is achieved by the refrigerant mixture having a sufficiently large proportion of heavier hydrocarbons depending on the selected method parameters.
4. A method according to claim 1, whereby the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated off.
5. A method according to claim 4, whereby the separated resulting liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit.
6. A method according to claim 5, whereby the forwarding is carried out by means of a pump
7. A method according to claim 1, whereby the refrigerant mixture fractions are not superheated.
8. A method according to claim 2, whereby incomplete vaporising of the refrigerant mixture is achieved by the refrigerant mixture having a sufficiently large proportion of heavier hydrocarbons depending on the selected method parameters.
9. A method according to claim 1, whereby incomplete vaporising of the refrigerant mixture is achieved by the refrigerant mixture having a sufficiently large proportion of heavier hydrocarbons, preferably C4H10— and C5H12— hydrocarbons, depending on the selected method parameters, such as vaporising temperature and pressure.
10. A method according to claim 2, whereby incomplete vaporising of the refrigerant mixture is achieved by the refrigerant mixture having a sufficiently large proportion of heavier hydrocarbons, preferably C4H10— and C5H12— hydrocarbons, depending on the selected method parameters, such as vaporising temperature and pressure.
11. A method according to claim 2, whereby the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated off.
12. A method according to claim 3, whereby the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated off.
13. A method according to claim 8, whereby the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated off.
14. A method according to claim 9, whereby the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated off.
15. A method according to claim 10, whereby the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated off.
16. A method according to claim 11, whereby the separated resulting liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit.
17. A method according to claim 12, whereby the separated resulting liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit.
18. A method according to claim 13, whereby the separated resulting liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit.
19. A method according to claim 14, whereby the separated resulting liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit.
20. A method according to claim 15, whereby the separated resulting liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit.
US12/438,500 2006-08-24 2007-08-24 Method for liquefying a hydrocarbon-rich flow Abandoned US20100115990A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102006039661A DE102006039661A1 (en) 2006-08-24 2006-08-24 Process for liquefying a hydrocarbon-rich stream
DE102006039661.8 2006-08-24
PCT/EP2007/058818 WO2008023059A2 (en) 2006-08-24 2007-08-24 Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes

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US20100115990A1 true US20100115990A1 (en) 2010-05-13

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US (1) US20100115990A1 (en)
AU (1) AU2007287506B2 (en)
DE (1) DE102006039661A1 (en)
GB (1) GB2454383B (en)
WO (1) WO2008023059A2 (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITMI20091768A1 (en) * 2009-10-15 2011-04-16 Ecoproject Sas Di Luigi Gazzi E C PROCESS FOR LNG PLANTS ALSO WITH LARGE CAPACITY ASKING FOR LOW VOLUMETRIC REACHES TO REFRIGERATING COMPRESSORS

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US1781541A (en) * 1926-12-16 1930-11-11 Electrolux Servel Corp Refrigeration
US4033735A (en) * 1971-01-14 1977-07-05 J. F. Pritchard And Company Single mixed refrigerant, closed loop process for liquefying natural gas
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
US4180123A (en) * 1977-02-14 1979-12-25 Phillips Petroleum Company Mixed-component refrigeration in shell-tube exchanger
US4229195A (en) * 1978-05-09 1980-10-21 Linde Aktiengesellschaft Method for liquifying natural gas
US4339253A (en) * 1979-12-12 1982-07-13 Compagnie Francaise D'etudes Et De Construction "Technip" Method of and system for liquefying a gas with low boiling temperature
US5414190A (en) * 1992-11-06 1995-05-09 Linde Aktiengesellschaft Process to recover liquid methane
US5602293A (en) * 1992-10-16 1997-02-11 Linde Aktiengesellschaft Process for separating a feedstock stream essentially consisting of hydrogen, methane and C3 /C4 -hydrocarbons
US6250105B1 (en) * 1998-12-18 2001-06-26 Exxonmobil Upstream Research Company Dual multi-component refrigeration cycles for liquefaction of natural gas
US6253574B1 (en) * 1997-04-18 2001-07-03 Linde Aktiengesellschaft Method for liquefying a stream rich in hydrocarbons
US6334334B1 (en) * 1997-05-28 2002-01-01 Linde Aktiengesellschaft Process for liquefying a hydrocarbon-rich stream
US6370910B1 (en) * 1998-05-21 2002-04-16 Shell Oil Company Liquefying a stream enriched in methane
US6389844B1 (en) * 1998-11-18 2002-05-21 Shell Oil Company Plant for liquefying natural gas
US20050013722A1 (en) * 2001-11-19 2005-01-20 Akira Usami Low alloy steel excellent in resistance to corrosion by hydrochloric acid and corrosion by sulfuric acid and weld joint comprising the same
US7228714B2 (en) * 2004-10-28 2007-06-12 Praxair Technology, Inc. Natural gas liquefaction system

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GB1572900A (en) * 1976-04-21 1980-08-06 Shell Int Research Process of the liquefaction of natural gas
US4548629A (en) * 1983-10-11 1985-10-22 Exxon Production Research Co. Process for the liquefaction of natural gas
DE19937623B4 (en) * 1999-08-10 2009-08-27 Linde Ag Process for liquefying a hydrocarbon-rich stream
DE102004032710A1 (en) * 2004-07-06 2006-02-09 Linde Ag Method for liquefying a hydrocarbon-rich stream, especially a natural gas stream, comprises separating a first coolant mixture cycle into a low boiling fraction and a higher boiling fraction
DE102005038266A1 (en) * 2005-08-12 2007-02-15 Linde Ag Process for liquefying a hydrocarbon-rich stream
US20090241593A1 (en) * 2006-07-14 2009-10-01 Marco Dick Jager Method and apparatus for cooling a hydrocarbon stream

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1781541A (en) * 1926-12-16 1930-11-11 Electrolux Servel Corp Refrigeration
US4033735A (en) * 1971-01-14 1977-07-05 J. F. Pritchard And Company Single mixed refrigerant, closed loop process for liquefying natural gas
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
US4180123A (en) * 1977-02-14 1979-12-25 Phillips Petroleum Company Mixed-component refrigeration in shell-tube exchanger
US4229195A (en) * 1978-05-09 1980-10-21 Linde Aktiengesellschaft Method for liquifying natural gas
US4339253A (en) * 1979-12-12 1982-07-13 Compagnie Francaise D'etudes Et De Construction "Technip" Method of and system for liquefying a gas with low boiling temperature
US5602293A (en) * 1992-10-16 1997-02-11 Linde Aktiengesellschaft Process for separating a feedstock stream essentially consisting of hydrogen, methane and C3 /C4 -hydrocarbons
US5414190A (en) * 1992-11-06 1995-05-09 Linde Aktiengesellschaft Process to recover liquid methane
US6253574B1 (en) * 1997-04-18 2001-07-03 Linde Aktiengesellschaft Method for liquefying a stream rich in hydrocarbons
US6334334B1 (en) * 1997-05-28 2002-01-01 Linde Aktiengesellschaft Process for liquefying a hydrocarbon-rich stream
US6370910B1 (en) * 1998-05-21 2002-04-16 Shell Oil Company Liquefying a stream enriched in methane
US6389844B1 (en) * 1998-11-18 2002-05-21 Shell Oil Company Plant for liquefying natural gas
US6250105B1 (en) * 1998-12-18 2001-06-26 Exxonmobil Upstream Research Company Dual multi-component refrigeration cycles for liquefaction of natural gas
US20050013722A1 (en) * 2001-11-19 2005-01-20 Akira Usami Low alloy steel excellent in resistance to corrosion by hydrochloric acid and corrosion by sulfuric acid and weld joint comprising the same
US7228714B2 (en) * 2004-10-28 2007-06-12 Praxair Technology, Inc. Natural gas liquefaction system

Also Published As

Publication number Publication date
DE102006039661A1 (en) 2008-03-20
GB0901366D0 (en) 2009-03-11
GB2454383B (en) 2011-05-04
AU2007287506B2 (en) 2010-06-17
WO2008023059A3 (en) 2009-01-29
WO2008023059A8 (en) 2010-02-11
GB2454383A (en) 2009-05-06
WO2008023059A2 (en) 2008-02-28
AU2007287506A1 (en) 2008-02-28

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