AU2005303932B2 - Method for liquefying a hydrocarbon-rich flow - Google Patents
Method for liquefying a hydrocarbon-rich flow Download PDFInfo
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- AU2005303932B2 AU2005303932B2 AU2005303932A AU2005303932A AU2005303932B2 AU 2005303932 B2 AU2005303932 B2 AU 2005303932B2 AU 2005303932 A AU2005303932 A AU 2005303932A AU 2005303932 A AU2005303932 A AU 2005303932A AU 2005303932 B2 AU2005303932 B2 AU 2005303932B2
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- Prior art keywords
- coolant mixture
- hydrocarbon
- coolant
- flow
- circuit
- Prior art date
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- 229930195733 hydrocarbon Natural products 0.000 title claims description 32
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 32
- 238000000034 method Methods 0.000 title claims description 31
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 29
- 239000002826 coolant Substances 0.000 claims description 63
- 239000000203 mixture Substances 0.000 claims description 63
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 22
- 238000001816 cooling Methods 0.000 claims description 18
- 239000003345 natural gas Substances 0.000 claims description 11
- 238000004781 supercooling Methods 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000003949 liquefied natural gas Substances 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000001273 butane Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 238000013386 optimize process Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
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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
- F25J1/003—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—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
- F25J1/0217—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 at least a three level refrigeration cascade with at least one MCR cycle
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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
- F25J1/02—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
- F25J1/0217—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 at least a three level refrigeration cascade with at least one MCR cycle
- F25J1/0218—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 at least a three level refrigeration cascade with at least one MCR cycle with one or more SCR cycles, e.g. with a C3 pre-cooling cycle
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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
- F25J1/02—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.
- F25J1/029—Mechanically coupling of different refrigerant compressors in a cascade refrigeration system to a common driver
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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
- F25J1/02—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
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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
- F25J1/02—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.
- F25J1/0295—Shifting of the compression load between different cooling stages within a refrigerant cycle or within a cascade refrigeration system
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
Description
C:\NRPortbl\DCC\WAM\3329250_1.DOC-26/11/2010 Method for liquefying a hydrocarbon-rich flow The invention relates to a method for liquefying a hydrocarbon-rich flow, particularly a natural gas flow, said 5 hydrocarbon-rich flow being liquefied counter to a cascade comprising three coolant mixture circuits, the first of which is used for pre-cooling while the second one is used for liquefying and the third one is used for supercooling the liquefied hydrocarbon-rich flow. 10 In the following, the term "first coolant mixture circuit" shall always be understood to mean a carbon dioxide coolant circuit. 15 A generic method for liquefying a hydrocarbon-rich flow is disclosed in German patent application publication 197 16 415. Quoting the German patent application publication 197 16 415, its published contents are included in the published contents of this patent application. 20 Natural gas liquefaction systems are designed as either so called LNG Baseload Plants - that is, plants for the liquefaction of natural gas to supply natural gas as a primary energy source - or as so-called Peak Shaving Plants 25 - that is, plants for the liquefaction of natural gas to cover peak demand. LNG Baseload Plants are typically operated with coolant circuits that consist of carbon dioxide mixtures. These 30 mixture circuits are energetically more efficient than expander circuits, and allow relatively low energy C \NRPOrtb1\DCC\kAM\3329250.1.DOC-26/11/2010 -2 consumption for the large liquefaction capacity of the baseload plants. In generic liquefaction methods, the first mixture circuit 5 is fundamentally used for pre-cooling; the second mixture circuit and the third mixture circuit are used for supercooling the hydrocarbon-rich flow or natural gas. Separation of higher volatility hydrocarbons takes place 10 to the extent necessary - between pre-cooling and liquefaction. These are mainly those components of the hydrocarbon-rich flow or natural gas that would freeze out in the next cooling - that is, C5+ hydrocarbons and aromatics. In addition, those hydrocarbons - particularly 15 propane and butane - that would cause an undesired increase in the heat value of the liquefied natural gas are often separated prior to liquefaction. In German patent application 103 44 030, a generic method is 20 also disclosed; with said method, at least part of the flow of the coolant mixture of the second coolant mixture circuit is used for pre-cooling the hydrocarbon-rich flow. The liquefaction method described in the German patent application 103 44 030 allows more economical use of the 25 available compressors and drives, since the (circuit) compressors of the three mixture circuits have approximately the same drive power; that is, about 33.33% of the total drive power. This allows particularly large liquefaction plants, with a liquefaction capacity of over 5 million tons 30 of LNG per year, to be operated more economically, since the liquefaction capacity of the liquefaction process can be C:\NRPortbl\DCC\WAM\3329250 1.DOC-26/11/2010 -3 maximized by using identical, proven drives and compressors in the three coolant circuits. Fundamentally, compressor drives and particularly gas 5 turbines are available only in discrete steps. For an intended plant size or liquefaction capacity, the use of three nearly identical or identical drives is often not suitable. 10 In particular, for cool environmental conditions - that is, conditions at which the air or coolant water temperature is below 15 to 20 OC - the portion of the required energy consumption needed for pre-cooling is reduced, to the extent that the use of the method as described in the above German 15 patent application 103 44 030 can no longer be considered optimal. One or more embodiments of the present invention may present a generic method that allows optimized process operation 20 with regard to the required energy consumption, even under the conditions given above. The present invention provides a method for liquefying a hydrocarbon-rich flow, particularly a natural gas flow, said 25 hydrocarbon-rich flow being liquefied counter to a cascade comprising first, second and third coolant mixture circuits, the first coolant mixture circuit being used for pre cooling, the second coolant mixture circuit being used for liquefying and the third coolant mixture circuit being used 30 for supercooling the liquefied hydrocarbon-rich flow; wherein the coolant mixture of the third coolant mixture C:\NRPorLbl\DCC\WAM\3329250_1.DOC-26/11/2010 -4 circuit is compressed using two essentially equal power compressors and the coolant mixture of each of the first and second coolant mixture circuits is compressed using a compressor that is essentially identical to the two 5 essentially equal power compressors of the third coolant mixture circuit. Using the method according to the invention, the compressor power, and thus the drive power, is distributed such that 10 less cooling power is available for pre-cooling the hydrocarbon-rich flow or natural gas flow to be liquefied. The total required power of the three coolant mixture circuits can now be distributed across four compressor drives. 15 The method of operation according to the invention may be particularly advantageous for single-pass liquefaction plants with a large capacity. 20 Expanding on the method according to the invention for liquefying a hydrocarbon-rich flow, in some embodiments it is proposed that the compressors in the first and second coolant mixture circuits and the compressor in the third coolant mixture circuit are driven by identical and/or equal 25 power drives. This arrangement of the method according to the invention is particularly sensible if compressor drives are available that can provide 50% of the required total power. In this 30 case, the compressors in the pre-cooling and liquefaction circuits and the compressors in the supercooling circuit can C:\NRPortl\DCC\WAM\J329250.1.DOC-25/11/2010 -5 be combined into two drive chains of identical or largely identical power. The terms "compressors with essentially identical power" and 5 "essentially identical and/or equal power drives" are used to mean drives with power that differs by no more than +/ 2%. Embodiments of the method according to the invention are 10 described, by way of example only, in closer detail using the application example shown in the figure. In the method described in the figure, cooling and liquefaction of the hydrocarbon-rich flow, which is fed into 15 the heat exchanger El via line 1, take place counter to a coolant mixture circuit cascade comprising three coolant mixture circuits. These typically are constructed in different ways, for instance as described in the above German patent application publication 197 16 415. 20 The hydrocarbon-rich flow to be liquefied is cooled in heat exchanger El counter to the two evaporating partial coolant mixture flow 4b and 4d of the first mixture circuit 4a to 4e, and the evaporating partial coolant flow 3d of the 25 second mixture circuit 3a to 3e, and then fed into the separation unit S, shown simply as a black box. To the extent that a (carbon dioxide) coolant circuit is used as an alternative to the first coolant mixture circuit, 30 the partial flow drawn off by line 4d and 4e is eliminated.
C:\NRftrtbl\DCC\WAM\33292SO_ 1. DOC-26/11/2010 - Sa Furthermore, in this case the compressor V4 has no side inlet, as is shown in the figure. The previously described separation of C3+ takes place in 5 the separation unit S, whereby the components separated from the hydrocarbon-rich flow to be liquefied are drawn off from the separation unit S via line 1b.
6 At least one partial flow, of the two partial flows 3b and 3d of the second coolant mixture circuit 3a to 3e, which is described in more detail below, is generally used to provide cold in the separation unit S. Here the 5 selection of which of the two partial flows 3b and/or 3d, is put to use as the at least one partial flow for this cold provision, will be determined by the temperature level(s) required in the separation unit S. 10 The hydrocarbon-rich flow to the liquefied is then fed into a second heat exchanger E2 via line lc, and liquefied therein counter to the evaporating partial coolant mixture flow 3b of the second coolant circuit 3a to 3b. 15 After liquefaction is complete, the hydrocarbon-rich flow is fed into a third exchanger E3 via line ld, and supercooled therein counter to the coolant mixture flow 2b of the third coolant circuit 2a to 2c. The supercooled 20 liquid product is then fed through line le to its further use and/or (intermediate) storage. In contrast to the method described in the above German patent application 103 44 030, the supercooling cold 25 circuit 2a to 2c, according to the invention, now comprises two compressors V2 and V2' in series. The pre cooling and liquefaction cold circuits have only one compressor each, V4 or V3. The compressors used, V2, V2', V3, and V4, are also identical in power, according to the 30 invention, and essentially identical in design. This means that the power requirement of each compressor V2, V2', V3 and V4, and compressor drive A2, A2', A3, and A4, C:\NRPortbl\DCC\WAM\3329250_1.DOC-26/11/2010 -7 provides 25%, at least between 23% and 27%, of the total power. Gas or steam turbines or electric motors may be used advantageously as drive A2, A2' , A3, and A4 for the compressors 5 V2, V2', V3, and V4. Not shown in the figure are the coolers or heat exchangers downstream of the compressors V2, V2', V3, and V4, in which the coolant mixture is cooled counter to a coolant medium - such as 10 water - and, in the case of the first coolant (mixture) circuit 4a to 4e, is condensed. The coolant mixture compressed in compressor V4 in the first mixture circuit is fed into the heat exchanger El via line 4a, 15 and, after cooling is complete, divided therein into two partial flows 4b and 4d. Once expansion has taken place in the valves d and e or the expansion devices, the coolant mixture in these partial flows 4b and 4d is evaporated to different pressure levels in heat exchanger El, then fed into the compressor V4 20 before the first stage (partial flow 4c) or at an intermediate pressure level (partial flow 4e) via line 4c or 4e. The coolant mixture compressed in compressor V3 in the second coolant circuit 3a to 3e is fed through heat exchangers El and E2 25 via line 3a and cooled therein. That partial flow 3b of this coolant mixture flow, which is fed through heat exchanger E2, is evaporated after expansion in valve b in heat exchanger E2 counter to process flows to be cooled, and then fed into the input stage of compressor V3 via line 3c.
8 One partial flow 3d of the coolant mixture of the second coolant mixture circuit 3a to 3e is drawn off to heat exchanger El, expanded in valve c, and then evaporated in heat exchanger El counter to process flows to be cooled, 5 before this partial coolant mixture flow is fed into the circuit compressor V3 via line 3e at an intermediate pressure level. This partial coolant mixture flow 3d thus contributes to pre-cooling the hydrocarbon-rich flow in heat exchanger El. 10 In order to be able to achieve this, the partial flow 3d of the coolant mixture of the second coolant mixture circuit 3a to 3e used for pre-cooling the hydrocarbon rich flow must be evaporated to a pressure that is higher 15 than the evaporation pressure of the partial coolant mixture flow 3b of the second coolant mixture circuit 3a to 3e. By selecting the intermediate pressure at which the 20 coolant mixture flow 3e is evaporated and fed into the compressor V3, and by regulating the mass distribution of the two partial coolant mixture flows 3b and 3d, the division of cooling power of the second mixture circuit between heat exchangers El and E2, and thereby between 25 pre-cooling and liquefaction of the hydrocarbon-rich flow to be liquefied, can be adjusted nearly as desired. Expanding on the method according to the invention for liquefying a hydrocarbon-rich flow, it is proposed that 30 the compressors V4 and V3 of the first and second coolant mixture circuits and the compressors V2 and V2' of the third coolant mixture circuit are driven by two essentially identical or equal power drives.
C: \NRPortbl\DCC\WAM\33292501 .DOC-26/11/2010 -9 This arrangement of the method according to the invention, not shown in the figure, may be particularly advantageous if the total power of the compressors V2, V2',- V3, and V4 is provided by two sufficiently powerful drives. The plant availability is 5 generally higher if the number of drives required for operation is minimized, which is the case if only two drives are used instead of four. The method for liquefying a hydrocarbon-rich flow, particularly a 10 natural gas flow, according to the invention, may thus allow even more economical use of the available compressors and drives than is possible with the known liquefaction processes. Particularly large, single-pass liquefaction plant with a liquefaction capacity of more than 5 million tons of LNG per year may profit 15 from the method according to the invention. Throughout this specification and the claims which follow, unless the context requires otherwise, the word "comprise", and variations such as "comprises" and "comprising", will be 20 understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step or group of integers or steps. The reference in this specification to any prior publication (or 25 information derived from it), or to any matter which is known, is not, and should not be taken as an acknowledgment or admission or any form of suggestion that that prior publication (or information derived from it) or known matter forms part of the common general knowledge in the field of endeavour to which this 30 specification relates.
Claims (5)
1. Method for liquefying a hydrocarbon-rich flow, said hydrocarbon-rich flow being liquefied counter to a 5 cascade comprising first, second and third coolant mixture circuits, the first coolant mixture circuit being used for pre-cooling, the second coolant mixture circuit being used for liquefying and the third coolant mixture circuit being used for supercooling the 10 liquefied hydrocarbon-rich flow; wherein the coolant mixture of the third coolant mixture circuit is compressed using two essentially equal power compressors and the coolant mixture of each of the first and second coolant mixture circuits is compressed using a 15 compressor that is essentially identical to the two essentially equal power compressors of the third coolant mixture circuit.
2. Method as in claim 1, wherein the compressors of the 20 first and second coolant mixture circuits and the compressors of the third coolant mixture circuit are driven by two essentially identical and/or equal power drives. 25
3. Method as in claim 1 or 2, wherein gas or steam turbines and/or electric motors are used as drives for the compressors of the first, second and third coolant mixture circuits. 30
4. A method according to claim 1, 2 or 3, wherein the hydrocarbon-rich flow is a natural gas flow. C:\NRPortbl\DCC\WAM\3329250_1.DOC-26/11/2010 - 11
5. A method for liquefying a hydrocarbon-rich flow, substantially as hereinbefore described with reference to the accompanying drawing.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102004054674.6 | 2004-11-12 | ||
| DE200410054674 DE102004054674A1 (en) | 2004-11-12 | 2004-11-12 | Process for liquefying a hydrocarbon-rich stream |
| PCT/EP2005/011948 WO2006050913A1 (en) | 2004-11-12 | 2005-11-08 | Method for liquefying a hydrocarbon-rich flow |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2005303932A1 AU2005303932A1 (en) | 2006-05-18 |
| AU2005303932B2 true AU2005303932B2 (en) | 2010-12-23 |
Family
ID=35539700
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2005303932A Active AU2005303932B2 (en) | 2004-11-12 | 2005-11-08 | Method for liquefying a hydrocarbon-rich flow |
Country Status (6)
| Country | Link |
|---|---|
| CN (1) | CN100535563C (en) |
| AU (1) | AU2005303932B2 (en) |
| DE (1) | DE102004054674A1 (en) |
| NO (1) | NO20072961L (en) |
| RU (1) | RU2373465C2 (en) |
| WO (1) | WO2006050913A1 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102005029275A1 (en) * | 2005-06-23 | 2006-12-28 | Linde Ag | Method for liquefying hydrocarbon-rich flow, in particular flow of natural gas first and second refrigerant-mixture circuits for precooling hydrocarbon-rich flow and third refrigerant-mixture circuit for liquefying and supercooling flow |
| WO2008015224A2 (en) * | 2006-08-02 | 2008-02-07 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for liquefying a hydrocarbon stream |
| CN101688752B (en) * | 2007-07-12 | 2012-09-05 | 国际壳牌研究有限公司 | Method and apparatus for cooling a hydrocarbon stream |
| CN102393126B (en) * | 2011-10-25 | 2013-11-06 | 中国寰球工程公司 | Natural gas liquefaction system and method with bi-circulating mixed refrigerant |
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| EP3361197A1 (en) | 2017-02-14 | 2018-08-15 | Linde Aktiengesellschaft | Method for the liquefaction of a fraction rich in hydrocarbon |
| EP3361196A1 (en) | 2017-02-14 | 2018-08-15 | Linde Aktiengesellschaft | Method for the liquefaction of a fraction rich in hydrocarbon |
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- 2005-11-08 CN CNB2005800386985A patent/CN100535563C/en not_active Expired - Fee Related
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- 2005-11-08 AU AU2005303932A patent/AU2005303932B2/en active Active
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Also Published As
| Publication number | Publication date |
|---|---|
| NO20072961L (en) | 2007-06-11 |
| AU2005303932A1 (en) | 2006-05-18 |
| RU2007121845A (en) | 2008-12-20 |
| RU2373465C2 (en) | 2009-11-20 |
| WO2006050913A1 (en) | 2006-05-18 |
| CN101057117A (en) | 2007-10-17 |
| CN100535563C (en) | 2009-09-02 |
| DE102004054674A1 (en) | 2006-05-24 |
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