AU2010238844B2 - Method for liquefying a hydrocarbon-rich fraction - Google Patents

Method for liquefying a hydrocarbon-rich fraction Download PDF

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AU2010238844B2
AU2010238844B2 AU2010238844A AU2010238844A AU2010238844B2 AU 2010238844 B2 AU2010238844 B2 AU 2010238844B2 AU 2010238844 A AU2010238844 A AU 2010238844A AU 2010238844 A AU2010238844 A AU 2010238844A AU 2010238844 B2 AU2010238844 B2 AU 2010238844B2
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mixed refrigerant
cycle
hydrocarbon
rich fraction
liquefying
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AU2010238844A1 (en
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Heinz Bauer
Hubert Franke
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Linde GmbH
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Linde GmbH
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—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
    • F25J1/0002—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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0085—Ethane; Ethylene
    • 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
    • F25J1/008—Hydrocarbons
    • F25J1/0087—Propane; Propylene
    • 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
    • F25J1/0095—Oxides of carbon, e.g. CO2
    • 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
    • F25J1/0214—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 dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—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 dual level refrigeration cascade with at least one MCR cycle with one 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
    • F25J1/0211—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
    • F25J1/0214—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 dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—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 dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
    • F25J1/0216—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 dual level refrigeration cascade with at least one MCR cycle with one SCR cycle using a C3 pre-cooling cycle

Abstract

A method for liquefying a hydrocarbon-rich fraction is described. According to the invention, the hydrocarbon-rich fraction (1, 2) is cooled (E6) and liquefied (E7) in an indirect heat exchange with the coolant mixture of a coolant mixture cycle (5-9), the hydrocarbon-rich fraction (1, 2) is cooled (E6) in an indirect heat exchange with the fully evaporated coolant mixture of the coolant mixture cycle (5-9), the compressed coolant mixture of the coolant mixture cycle (5-9) is precooled using a pure-substance refrigeration cycle (10-19), and the composition of the coolant mixture and/or the final compressor pressure of the coolant mixture cycle (5-9) is/are selected such that all of the coolant mixture is liquefied by the pure-substance refrigeration cycle (10-19).

Description

1 Method for liquefying a hydrocarbon-rich fraction The invention relates to a method for liquefying a hydrocarbon-rich fraction. US 3,763,658 discloses a method for liquefying a hydrocarbon-rich fraction which is used, in particular, in natural gas liquefaction processes. In this case a mixed refrigerant cycle serves for liquefying and subcooling the natural gas, while a single component cycle is additionally provided which not only precools the natural gas which is to be liquefied but also precools and partially liquefies the mixed refrigerant of the mixed refrigerant cycle. Such a liquefaction method is suitable, in particular, for natural gas liquefaction processes having an output between 1 and 6 million tons of LNG per year. The natural gas which is to be liquefied, before the actual cooling and liquefaction, is generally fed to an aqueous amine scrubber, downstream of which a drying unit is customarily connected. In particular in warm climatic zones, a substream of the above described single-component cycle can be used for condensation of water present in the natural gas, which relieves the drier connected downstream of the amine scrubber. This liquefaction process, however, requires a comparatively high amount of resources of apparatus. For instance, depending on the design, up to nine single-component evaporators of the kettle type and also two helically coiled heat exchanger bundles must be provided. In particular in the case of relatively small liquefaction outputs these may be taken to mean outputs of less than 3 million tons of LNG per year- the above-described process procedure has disadvantages compared with what are termed the Single Mixed Refrigerant (SMR) liquefaction processes which do not have a separate precooling circuit, since the above described liquefaction process gives rise to higher capital costs which cannot be compensated even by the lower energy consumption thereof. Any discussion of the prior art throughout the specification should in no way be considered as an admission that such prior art is widely known or forms part of common general knowledge in the field. It is an object of the present invention to overcome or ameliorate at least one of the disadvantages of the prior art, or to provide a useful alternative. It is an object of preferred embodiments of the present invention to specify a method of the type in question for liquefying a hydrocarbon-rich fraction which avoids the above-described disadvantages.
2 According to a first aspect of the invention, there is provided a method for liquefying a hydrocarbon- rich fraction, which comprises a) cooling and liquefying the hydrocarbon-rich fraction in indirect heat exchange against the mixed refrigerant of a mixed refrigerant cycle, b) cooling the hydrocarbon-rich fraction in indirect heat exchange against the total vaporized mixed refrigerant of the mixed refrigerant cycle, c) precooling the compressed mixed refrigerant of the mixed refrigerant cycle by means of a single-component refrigeration cycle, and d) selecting the composition of the mixed refrigerant and/or the final compressor pressure of the mixed refrigerant cycle in such a manner that the mixed refrigerant is totally liquefied by the single-component refrigeration cycle. Unless the context clearly requires otherwise, throughout the description and the claims, the words "comprise", "comprising", and the like are to be construed in an inclusive sense as opposed to an exclusive or exhaustive sense; that is to say, in the sense of "including, but not limited to". According to a second aspect of the invention, there is provided a liquefied hydrogen-rich fraction produced by the method according to the first aspect. The expression "single-component refrigeration cycle" may be taken to mean a refrigeration cycle in which the refrigerant is present in a concentration of at least 95% by volume. In contrast to the above-described liquefaction method, cooling and liquefaction of the hydrocarbon-rich fraction now proceed exclusively in indirect heat exchange against the mixed refrigerant of a mixed refrigerant cycle. The single-component refrigeration cycle which must be additionally provided serves according to the invention solely for precooling the compressed mixed refrigerant of the mixed refrigerant cycle. In this case, the composition of the mixed refrigerant and/or the final compressor pressure of the mixed refrigerant cycle must be selected in such a manner that the mixed refrigerant can be cooled by the single-component refrigeration cycle to the extent that it is present in totally liquefied form. As a consequence thereof, the mixed refrigerant can be fed directly to a heat exchanger which serves for liquefying and subcooling the hydrocarbon-rich fraction, without a separator needing to be connected upstream of this heat exchanger.
3 In the case of the procedure according to the invention, nevertheless, the advantage of precooling by means of a single-component refrigeration cycle with respect to energy consumption and suitability for relieving any drying unit to be provided can be essentially retained. The expenditure on apparatus of the liquefaction method 5 according to the invention is significantly less compared with the above-described liquefaction method, however, since the number of heat exchangers is markedly reduced. Although the procedure according to the invention leads to a slight increase in energy 10 consumption - the increase is a maximum of 5% - the total economic efficiency of the liquefaction process improves, for which reason the procedure according to the invention is more economical than known liquefaction processes, in particular in the output range between 0.5 and 3 million tons of LNG per year. 15 Further advantageous embodiments of the method according to the invention for liquefying a hydrocarbon-rich fraction which are subjects of the dependent claims are characterized in that - the refrigerant of the single-component refrigeration cycle comprises at least 20 95% by volume of C 3
H
8 , C 3
H
6 , C 2
H
6 , C 2
H
4 or C02, - the mixed refrigerant of the mixed refrigerant cycle contains nitrogen, methane and at least two of the components from the group C 2
H
4 , C 2
H
6 , C 3
H
8 , C 4 H1 0 , and
C
5
H
12 , and 25 - the mixed refrigerant of the mixed refrigerant cycle totally vaporizes during the liquefaction of the hydrocarbon-rich fraction. The method according to the invention for liquefying a hydrocarbon-rich fraction and 30 also further advantageous embodiments thereof which are subjects of the dependent claims will be described in more detail hereinafter with reference to the exemplary embodiment shown in the figure. Via line 1, the hydrocarbon-rich fraction which is to be liquefied, which hereinafter is 35 intended to be a natural gas stream, is fed to an amine scrubber A. Connected 4 downstream of this is a drying unit T, upstream of which is a heat exchanger El. In this heat exchanger, to relieve the drying unit T, partial condensation of water contained in the natural gas is effected. 5 The thus pretreated natural gas stream is fed via line 2 to a heat exchanger E6 and cooled in this against the totally vaporized mixed refrigerant of the mixed refrigerant cycle, which will be considered further hereinafter. The heat exchanger E6 is preferably constructed as a plate heat exchanger. 10 Via line 3, the cooled natural gas stream is fed to a heat exchanger E7, which is preferably constructed as a helically coiled heat exchanger. In this the natural gas stream is liquefied and subcooled in indirect heat exchange with the mixed refrigerant of the mixed refrigerant cycle. Via line 4, the subcooled LNG product stream is taken off and fed to temporary storage or directly to further use thereof. 15 The mixed refrigerant of the mixed refrigerant cycle is compressed to the desired final compressor pressure in a single-stage or multistage compressor unit; the figure shows two compressor stages V2 and V2', wherein, between the compressor stages, an intercooler which is not shown in the figure is preferably provided. After it is cooled in 20 the aftercooler E9, the compressed mixed refrigerant is conducted via the line 5 through four series-connected heat exchangers E2 to E5. In these the mixed refrigerant is cooled in indirect heat exchange with the refrigerant of the single-component refrigeration cycle, which will be considered in more detail hereinafter, to the extent that it is liquid, and therefore present as a single phase, at the exit of the last heat 25 exchanger ES. In order to achieve this total condensation of the mixed refrigerant of the mixed refrigerant cycle at the exit of the last heat exchanger E5, the composition of the mixed refrigerant and/or the final compressor pressure of the mixed refrigerant cycle must be 30 chosen appropriately. As refrigerant for the single-component refrigeration cycle, C 3
H
8 , C 3
H
6 , C 2 He, C 2
H
4 or
CO
2 is preferably used. The mixed refrigerant of the mixed refrigerant cycle preferably contains nitrogen, methane and at least two of the components of the group C 2
H
4 , 35 C 2
H
6 , C 3
H
8 , C 4
H
10 and C 5
H
12
.
5 The mixed refrigerant liquefied by the single-component refrigeration cycle can then be fed directly to the heat exchanger E7 via the line 6. This makes unnecessary the provision of a separator connected upstream of the heat exchanger E7. In the heat 5 exchanger E7 the liquid mixed refrigerant is subcooled before it is taken off via line 7 and expanded to the lowest pressure in the valve a. Alternatively to the valve a shown in the figure, a liquid expander can be provided which serves for the work-producing expansion of the mixed refrigerant at the cold end 10 of the heat exchanger E7. The mixed refrigerant which is expanded and fed back to the heat exchanger E7 via line 7 serves in the heat exchanger E7 for liquefying and subcooling the natural gas stream. Advantageously, the mixed refrigerant vaporizes totally during the liquefaction 15 and subcooling of the natural gas stream, and so a totally vaporized mixed refrigerant stream is taken off from the heat exchanger E7 via line 8 and fed to the heat exchanger E6. In this the mixed refrigerant is superheated against the natural gas stream which is to be cooled, before the mixed refrigerant is fed back via line 9 to the intake of the cycle compressor unit V2N2'. 20 The abovementioned single-component refrigeration cycle likewise has a multistage compressor unit V1 to which a liquefier E8 is assigned. The refrigerant which is compressed to the desired end pressure is fed via line 10 to a branch point at which a substream of the refrigerant is expanded via the valve b into the abovementioned heat 25 exchanger El and from this is fed back to the compressor unit V1 via the lines 11 and 13. A second substream is expanded into the heat exchanger E2 via line 12 and valve c. While the gaseous proportion of the refrigerant is taken off from the heat exchanger E2 30 via line 13 and fed to the compressor unit V1 at an intermediate pressure stage, the liquid proportion of the refrigerant is taken off from the heat exchanger E2 via line 14 and expanded into the heat exchanger E3 via valve d. Again there is a division into a gaseous refrigerant proportion which is fed to the compressor unit V1 via line 15 at an intermediate pressure stage, whereas the liquid refrigerant proportion is taken off via 35 line 16 and expanded into the heat exchanger E4 via valve e. From this heat 6 exchanger also the gaseous refrigerant proportion is fed via line 17 to the compressor unit V1 at an intermediate pressure stage, whereas the liquid refrigerant proportion is taken off via line 18 and expanded into the last heat exchanger E5 via valve f. Via line 19, the totally vaporized refrigerant is fed to the compressor unit V1 at the lowest 5 pressure stage. Instead of the cooling of the mixed refrigerant shown in the figure in the heat exchangers E2 to E5, in practice, also fewer than four heat exchangers can be implemented. The number of heat exchangers is essentially determined by the ambient 10 temperature and the number of impeller wheels in the turbocompressor V1. The method according to the invention for liquefying a hydrocarbon-rich fraction provides a liquefaction process which has an improved overall economic efficiency for reduced expenditure on apparatus, wherein this must be offset by a small increase in 15 energy consumption. The procedure according to the invention is suitable, in particular, for output ranges between 0.5 and 3 million tons of LNG per year.

Claims (5)

1. Method for liquefying a hydrocarbon-rich fraction, which comprises a) cooling and liquefying the hydrocarbon-rich fraction in indirect heat exchange against the mixed refrigerant of a mixed refrigerant cycle, b) cooling the hydrocarbon-rich fraction in indirect heat exchange against the total vaporized mixed refrigerant of the mixed refrigerant cycle, c) precooling the compressed mixed refrigerant of the mixed refrigerant cycle by means of a single-component refrigeration cycle, and d) selecting the composition of the mixed refrigerant and/or the final compressor pressure of the mixed refrigerant cycle in such a manner that the mixed refrigerant is totally liquefied by the single-component refrigeration cycle.
2. Method according to Claim 1, wherein the refrigerant of the single component refrigeration cycle comprises at least 95% by volume of C 3 H 8 , C 3 H 6 , C 2 H 6 , C 2 H 4 or C02.
3. Method according to Claim 1 or 2, wherein the mixed refrigerant of the mixed refrigerant cycle contains nitrogen, methane and at least two of the 20 components from the group C 2 H 4 , C 2 H 6 , C 3 H, C 4 H 1 0 . and C 5 H12
4. Method according to any one of the preceding Claims I to 3, wherein the mixed refrigerant of the mixed refrigerant cycle totally vaporizes during the liquefaction of the hydrocarbon-rich fraction.
5 A liquefied hydrogen-rich fraction produced by the method according to any one of claims 1 to 4.
AU2010238844A 2009-04-21 2010-04-15 Method for liquefying a hydrocarbon-rich fraction Active AU2010238844B2 (en)

Applications Claiming Priority (3)

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DE102009018248.9 2009-04-21
DE102009018248A DE102009018248A1 (en) 2009-04-21 2009-04-21 Process for liquefying a hydrocarbon-rich fraction
PCT/EP2010/002326 WO2010121752A2 (en) 2009-04-21 2010-04-15 Method for liquefying a hydrocarbon-rich fraction

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AU2010238844B2 true AU2010238844B2 (en) 2015-11-26

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AR (1) AR075917A1 (en)
AU (1) AU2010238844B2 (en)
BR (1) BRPI1013712B1 (en)
CL (1) CL2011002392A1 (en)
DE (1) DE102009018248A1 (en)
MY (1) MY173948A (en)
NO (1) NO346539B1 (en)
PE (1) PE20121108A1 (en)
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PE20121108A1 (en) 2012-08-03
AR075917A1 (en) 2011-05-04
NO20111495A1 (en) 2011-11-01
DE102009018248A1 (en) 2010-10-28
CN102575897A (en) 2012-07-11
BRPI1013712A2 (en) 2016-04-05
CN102575897B (en) 2014-11-26
WO2010121752A3 (en) 2012-10-11
WO2010121752A2 (en) 2010-10-28
AU2010238844A1 (en) 2011-09-15
BRPI1013712B1 (en) 2020-12-01
RU2011147065A (en) 2013-05-27
MY173948A (en) 2020-02-28
RU2568697C2 (en) 2015-11-20
NO346539B1 (en) 2022-09-26
CL2011002392A1 (en) 2012-02-10

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