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GB2454383A - Method for liquefying a hydrocarbon-rich flow - Google Patents

Method for liquefying a hydrocarbon-rich flow Download PDF

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Publication number
GB2454383A
GB2454383A GB0901366A GB0901366A GB2454383A GB 2454383 A GB2454383 A GB 2454383A GB 0901366 A GB0901366 A GB 0901366A GB 0901366 A GB0901366 A GB 0901366A GB 2454383 A GB2454383 A GB 2454383A
Authority
GB
United Kingdom
Prior art keywords
refrigerant mixture
hydrocarbon
vaporised
fractions
refrigerant
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
GB0901366A
Other versions
GB2454383B (en
GB0901366D0 (en
Inventor
Wolfgang Foerg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of GB0901366D0 publication Critical patent/GB0901366D0/en
Publication of GB2454383A publication Critical patent/GB2454383A/en
Application granted granted Critical
Publication of GB2454383B publication Critical patent/GB2454383B/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

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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
    • F25J1/02—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
    • F25J1/0002—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
    • 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

Landscapes

  • 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

Described is a method for liquefying a hydrocarbon-rich flow, in particular a natural gas 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. During normal operation the refrigerant mixture fractions are not fully vaporised and preferably also not overheated. Hereby at least 1 to 10 % by weight of the total quantity of the refrigerant mixture are not vaporised.

Description

METHOD FOR LIQUEFYING A HYDROCARBON-RICH FLOW
The invention relates to a method for liquefying a hydro- carbon-rich flow, in particular a natural gas flow, via indi- rect heat exchange with the refrigerant mixture of a refriger-ant 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 abovementjoned patent, are generally desig- nated as "Single-Flow Mixed Refrigerant Cycle". A common ele-ment 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 hy- drocarbon-rich flow it has been shown however that this heat-ing 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 un-wanted interruption of the liquefaction process.
Other generic methods for liquefying a hydrocarbon-rich flow are for example the so-called "Parallel Mixed Refriger-ant" method, as described for example in US patent 6,389,844; the so-called "Double Mixed Refrigerant" method, such as de- scribed for example in US patent 6,370,910; or other refriger- ant mixture methods with pre-cooling circuit, such as for ex-ample 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 mix-ture 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 re-frigerant mixture fractions are not fully vaporised.
A further advantageous accomplishment is that the ref rig-erarit mixture fractions are not superheated, in particular they are not superheated above their dew point, and more par-ticularly are not superheated by Ca. 10 K above their dew point.
In further advantageous configurations of the method ac-cording 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 mix-ture 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 re-frigerant mixture fractions is separated of f; 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 un-interruptedly in normal operation there is no complete vapor-ising 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 pro-vide at least one extra pump, by means of which the separated quantity of liquid or fraction resp. can be pumped to a suit-able site inside the refrigerant mixture circuit. Referring for example to Figure 1 of the abovementjoned 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 asso- ciated with the method according to the invention for liquefy- ing a hydrocarbon-rich flow, a not inconsiderable thermody-namic 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 en-thalpy 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 improve-ment in efficiency of the overall process.
The method can also be employed to advantage in other re-frigerant mixture methods for liquefying hydrocarbon-rich flow, in addition to the "Single-Flow Mixed Refrigerant Cycle method1'.

Claims (7)

  1. Claims 1. A method for liquefying a hydrocarbon-rich flow, in par-ticular a natural gas 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 recompres-sion, and whereby the refrigerant mixture fractions are not fully vaporised.
  2. 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. 3. A method according to claim 1 or 2, whereby incomplete Va- porising of the refrigerant mixture is achieved by the ref rig- erane mixture having a sufficiently large proportion of heav- ier hydrocarbons, preferably C4H10-and C5H12-hydrocarbons, de-pending on the selected method parameters, such as vaporising temperature and pressure.
  4. 4. A method according to any one of the preceding claims 1 to 3, whereby the liquid accruing from incomplete vaporising of the refrigerant mixture fractions is separated of f.
  5. 5. A method according to claim 4, whereby the separated re-sulting liquid is forwarded to a suitable supply point inside the refrigerant mixture circuit.
  6. 6. A method according to claim 5, whereby the forwarding is carried out by means of a pump.
  7. 7. A method according to any one of the preceding claims 1 to 6, whereby the refrigerant mixture fractions are not super-heated.
GB0901366A 2006-08-24 2007-08-24 Method for liquefying a hydrocarbon-rich flow Expired - Fee Related GB2454383B (en)

Applications Claiming Priority (2)

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

Publications (3)

Publication Number Publication Date
GB0901366D0 GB0901366D0 (en) 2009-03-11
GB2454383A true GB2454383A (en) 2009-05-06
GB2454383B GB2454383B (en) 2011-05-04

Family

ID=39078761

Family Applications (1)

Application Number Title Priority Date Filing Date
GB0901366A Expired - Fee Related GB2454383B (en) 2006-08-24 2007-08-24 Method for liquefying a hydrocarbon-rich flow

Country Status (5)

Country Link
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

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
GB1572900A (en) * 1976-04-21 1980-08-06 Shell Int Research Process of the liquefaction of natural gas
GB2147984A (en) * 1983-10-11 1985-05-22 Exxon Production Research Co A process for the liquefaction of natural gas
DE19937623A1 (en) * 1999-08-10 2001-02-15 Linde Ag Process for liquefying a hydrocarbon-rich stream e.g. natural gas, comprises carrying out indirect heat exchange with at least one cycle using a two-phase coolant mixture stream before compression
WO2007020252A2 (en) * 2005-08-12 2007-02-22 Wolfgang Foerg Method and arrangement for liquefying a stream rich in hydrocarbons
WO2008006867A2 (en) * 2006-07-14 2008-01-17 Shell Internationale Research Maatschappij B.V. Method and apparatus for cooling a hydrocarbon stream

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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
US4180123A (en) * 1977-02-14 1979-12-25 Phillips Petroleum Company Mixed-component refrigeration in shell-tube exchanger
DE2820212A1 (en) * 1978-05-09 1979-11-22 Linde Ag METHOD FOR LIQUIDATING NATURAL GAS
FR2471566B1 (en) * 1979-12-12 1986-09-05 Technip Cie METHOD AND SYSTEM FOR LIQUEFACTION OF A LOW-BOILING GAS
DE4235006A1 (en) * 1992-10-16 1994-04-21 Linde Ag Process for separating a feed stream consisting essentially of hydrogen, methane and C¶3¶ / C¶4¶ hydrocarbons
DE4237620A1 (en) * 1992-11-06 1994-05-11 Linde Ag Process for the production of high-purity liquid methane
DE19716415C1 (en) * 1997-04-18 1998-10-22 Linde Ag Process for liquefying a hydrocarbon-rich stream
DE19722490C1 (en) * 1997-05-28 1998-07-02 Linde Ag Single flow liquefaction of hydrocarbon-rich stream especially natural gas with reduced energy consumption
TW477890B (en) * 1998-05-21 2002-03-01 Shell Int Research Method of liquefying a stream enriched in methane
TW421704B (en) * 1998-11-18 2001-02-11 Shell Internattonale Res Mij B Plant for liquefying natural gas
MY117548A (en) * 1998-12-18 2004-07-31 Exxon Production Research Co Dual multi-component refrigeration cycles for liquefaction of natural gas
JP4319817B2 (en) * 2001-11-19 2009-08-26 新日本製鐵株式会社 Low alloy steel excellent in hydrochloric acid corrosion resistance and sulfuric acid corrosion resistance and its welded joint
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
US7228714B2 (en) * 2004-10-28 2007-06-12 Praxair Technology, Inc. Natural gas liquefaction system

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
GB1572900A (en) * 1976-04-21 1980-08-06 Shell Int Research Process of the liquefaction of natural gas
GB2147984A (en) * 1983-10-11 1985-05-22 Exxon Production Research Co A process for the liquefaction of natural gas
DE19937623A1 (en) * 1999-08-10 2001-02-15 Linde Ag Process for liquefying a hydrocarbon-rich stream e.g. natural gas, comprises carrying out indirect heat exchange with at least one cycle using a two-phase coolant mixture stream before compression
WO2007020252A2 (en) * 2005-08-12 2007-02-22 Wolfgang Foerg Method and arrangement for liquefying a stream rich in hydrocarbons
WO2008006867A2 (en) * 2006-07-14 2008-01-17 Shell Internationale Research Maatschappij B.V. Method and apparatus for cooling a hydrocarbon stream

Also Published As

Publication number Publication date
GB2454383B (en) 2011-05-04
DE102006039661A1 (en) 2008-03-20
WO2008023059A8 (en) 2010-02-11
WO2008023059A3 (en) 2009-01-29
AU2007287506B2 (en) 2010-06-17
US20100115990A1 (en) 2010-05-13
AU2007287506A1 (en) 2008-02-28
WO2008023059A2 (en) 2008-02-28
GB0901366D0 (en) 2009-03-11

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PCNP Patent ceased through non-payment of renewal fee

Effective date: 20150824