CN102762944A - 用于液化烃流的方法和设备 - Google Patents
用于液化烃流的方法和设备 Download PDFInfo
- Publication number
- CN102762944A CN102762944A CN2009801114011A CN200980111401A CN102762944A CN 102762944 A CN102762944 A CN 102762944A CN 2009801114011 A CN2009801114011 A CN 2009801114011A CN 200980111401 A CN200980111401 A CN 200980111401A CN 102762944 A CN102762944 A CN 102762944A
- Authority
- CN
- China
- Prior art keywords
- stream
- flow
- methane
- compressor
- terminal
- 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.)
- Pending
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 118
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 118
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 113
- 238000000034 method Methods 0.000 title claims abstract description 53
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 249
- 238000011084 recovery Methods 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 230000008859 change Effects 0.000 claims abstract description 9
- 239000002826 coolant Substances 0.000 claims description 123
- 238000001816 cooling Methods 0.000 claims description 59
- 239000012809 cooling fluid Substances 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 25
- 239000003345 natural gas Substances 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 24
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 230000001276 controlling effect Effects 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000000284 extract Substances 0.000 claims 1
- 239000003507 refrigerant Substances 0.000 abstract 9
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 20
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 17
- 239000003949 liquefied natural gas Substances 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 230000008569 process Effects 0.000 description 11
- 230000006835 compression Effects 0.000 description 10
- 238000007906 compression Methods 0.000 description 10
- 239000001294 propane Substances 0.000 description 10
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 9
- 239000001273 butane Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 7
- 235000019628 coolness Nutrition 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 5
- 238000005201 scrubbing Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910001868 water Inorganic materials 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 3
- -1 comprises methane Chemical compound 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 239000000659 freezing mixture Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 230000032258 transport Effects 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- MWRWFPQBGSZWNV-UHFFFAOYSA-N Dinitrosopentamethylenetetramine Chemical compound C1N2CN(N=O)CN1CN(N=O)C2 MWRWFPQBGSZWNV-UHFFFAOYSA-N 0.000 description 1
- 101000841267 Homo sapiens Long chain 3-hydroxyacyl-CoA dehydrogenase Proteins 0.000 description 1
- 102100029107 Long chain 3-hydroxyacyl-CoA dehydrogenase Human genes 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229940112112 capex Drugs 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- FEBLZLNTKCEFIT-VSXGLTOVSA-N fluocinolone acetonide Chemical compound C1([C@@H](F)C2)=CC(=O)C=C[C@]1(C)[C@]1(F)[C@@H]2[C@@H]2C[C@H]3OC(C)(C)O[C@@]3(C(=O)CO)[C@@]2(C)C[C@@H]1O FEBLZLNTKCEFIT-VSXGLTOVSA-N 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- JJYKJUXBWFATTE-UHFFFAOYSA-N mosher's acid Chemical compound COC(C(O)=O)(C(F)(F)F)C1=CC=CC=C1 JJYKJUXBWFATTE-UHFFFAOYSA-N 0.000 description 1
- GJVFBWCTGUSGDD-UHFFFAOYSA-L pentamethonium bromide Chemical compound [Br-].[Br-].C[N+](C)(C)CCCCC[N+](C)(C)C GJVFBWCTGUSGDD-UHFFFAOYSA-L 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
Images
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
- F25J1/0279—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
-
- 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
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0042—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by liquid expansion with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—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
- F25J1/003—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
- F25J1/0057—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 after expansion of the liquid refrigerant stream with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
- F25J1/0209—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop as at least a three level refrigeration cascade
- F25J1/021—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop as at least a three level refrigeration cascade using a deep flash recycle loop
-
- 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
-
- 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
-
- 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
- F25J1/0219—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 in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
-
- 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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
-
- 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
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
-
- 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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)
- Combustion & Propulsion (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
本发明公开了用于液化烃流的方法和设备。液化系统包括至少NGL回收系统12、主冷却剂回路42和第一冷却剂回路100、减压装置52,其后为终端气/液分离器62。主冷却剂回路42包括至少一个或多个主冷却剂压缩机45、45a、45b,并且所述第一冷却剂回路包括一个或多个第一冷却剂压缩机101。将烃进料流10传送经过所述NGL回收系统12,以产生富含甲烷的上部流20,其随后由所述第一和第二冷却剂回路冷却并液化。减小液化流的压力,并且将形成的混合相流60传送经过终端气/液分离器62,以形成终端气态流70和液化的烃产品流80。通过调节液化流的温度来改变终端气态流的量和通过控制以再循环流90b进给到富含甲烷的上部流20中的终端气态流的量,而将所述一个或多个主冷却剂压缩机和所述一个或多个第一冷却剂压缩机的负载功率最大化到其最大负载。
Description
技术领域
本发明涉及用于液化烃流例如天然气流的方法和设备。
背景技术
天然气为有用的燃料源,并且是众多烃化合物的来源。由于多种原因,通常期望在天然气流源处或附近的液化天然气(LNG)站中将天然气液化。例如,天然气以液态形式比以气态形式可能更易于存储或长途运输,因为液化天然气占据的体积小,并且不必在高压下存储。
通常,天然气,主要包括甲烷,在高压下进入LNG站,并且经预处理产生适于在低温下液化的纯化进料流。纯化的气体使用换热器经多个冷却步骤进行处理,以逐渐降低其温度,直到实现液化。然后液体天然气进一步冷却并且膨胀到适于存储和运输的最终大气压力。
除了甲烷之外,天然气通常包括一些较重的烃类和杂质,包括但不限于二氧化碳、硫、硫化氢和其他硫化合物、氮气、氦气、水、其他非烃酸性气体、乙烷、丙烷、丁烷、C5+烃和芳香烃。这些和任何其他常见或已知的重烃和杂质防碍或阻碍液化甲烷的常见已知方法,特别是最有效的液化甲烷的方法。大多数已知的或已提出的液化烃类的方法,特别是液化天然气的方法是基于在液化过程之前尽可能降低至少大部分重烃和杂质含量水平。
比甲烷并且通常比乙烷更重的烃类常常从天然气流冷凝并且回收为天然气液体(NGLs)。甲烷通常在高压洗涤塔中从NGLs分离,然后NGLs随后在多个专用精馏塔中分馏,来生产有价值的烃产品,或者以产品蒸气本身的形式,或者用于液化,例如作为冷却剂的组分。
同时,来自洗涤塔的甲烷随后液化来提供LNG。通过液化后减小压力并且分离,例如进行“终端闪蒸(end flash)”,能提供气态甲烷再循环流。
US 4,541,852描述了用于液化和低温冷却天然气的系统,其中,通过低温冷却LNG、减小压力和闪蒸LNG来回收气相天然气,从封闭的循环冷却液重新分配压缩功率。然后将气相天然气再压缩和再循环到系统的进料。
US 4,541,852的系统要求将通过对LNG进行减压和闪蒸而得到的气相天然气再压缩到815磅/平方英寸的进料流压力。因此需要高功率再压缩机驱动器。
US 4,541,852的系统不包括NGL提取系统。因而不可能通过将NGLs从进料流去除来改变LNG产品的规格。进料流中的在液化过程中可能固化的任何烃组分可能在系统中造成阻塞。
发明内容
在第一方面,本发明提供了一种液化烃流的方法,包括至少以下步骤:
(a)提供液化系统,其包括至少NGL回收系统、主冷却剂回路和第一冷却剂回路以及减压装置,减压装置之后为气/液分离器,所述主冷却剂回路包括至少一个或多个主冷却剂压缩机,并且所述第一冷却剂回路包括一个或多个第一冷却剂压缩机;
(b)将烃进料流传送经过所述NGL回收系统,以从所述烃进料流产生富含甲烷的上部流(overhead stream);
(c)将所述富含甲烷的上部流传送经过至少一第一压缩机,以形成压缩甲烷的流;
(d)借助于所述第一冷却剂回路中的第一冷却剂冷却所述压缩甲烷的流,随后借助于所述主冷却剂回路中的主冷却剂液化所述压缩甲烷的流,以形成第一液化流;
(e)减小所述第一液化流的压力,以形成混合相流;
(f)将所述混合相流传送经过终端气/液分离器,以形成终端气态流和液化的烃产品流;
(g)将所述终端气态流的至少再循环馏分进给到所述富含甲烷的上部流中或进给到在借助于所述第一冷却剂回路中的所述第一冷却剂进行的所述冷却的至少一部分上游的压缩甲烷的流中;
(h)通过调节第一液化流的温度(Tx)来改变来自终端气/液分离器的终端气态流的量和控制步骤(g)中进给的终端气态流的再循环馏分的量,将所述一个或多个主冷却剂压缩机和所述一个或多个第一冷却剂压缩机的负载功率最大化到其最大负载。
在第二方面,本发明提供了一种用于液化烃流的设备,所述设备至少包括:
-NGL回收系统,用于从烃进料流提取C2+流,以至少形成富含甲烷的上部流和富含C2+的下部流;
-至少一第一压缩机,用于从所述富含甲烷的上部流形成压缩甲烷的流;
-第一冷却级,用于冷却所述压缩甲烷的流,以形成冷却的压缩甲烷的流,随后是主冷却级,用于液化所述冷却的压缩甲烷的流,以形成第一液化流;
-减压装置,用于减小所述第一液化流的压力,以形成混合相流;
-终端气/液分离器,用于将所述混合相流分离为终端气态流和液化的烃产品流;以及
-再循环馏分管路,用于将所述终端气态流的至少再循环馏分进给到所述富含甲烷的上部流中;和
-控制系统,布置用于通过调节所述第一液化流的温度(Tx)来改变来自所述终端气/液分离器的所述终端气态流的量和控制所述再循环馏分管路中所述终端压缩流的再循环馏分的量,而将所述一个或多个主冷却剂压缩机和所述一个或多个第一冷却剂压缩机的负载功率最大化到其最大负载。
附图说明
现在将仅以举例的方式并且参照非限制性附图描述本发明的实施例和示例,附图中:
图1是一种液化烃流的方法的示意图;
图2是一种液化烃流的方法的更详细的示意图;
图3是另一个实施例的更详细的示意图;
图4是显示出控制器的一个实施例的示意图。
具体实施方式
对于本说明书而言,每条管路和该管路中运送的气流标注为单个附图标记。在整个本申请全文中,单位巴的使用应理解为指绝对压力。
本文描述了控制烃进料流液化的方法和用于此的设备,和/或最大化液化的烃流的生产的方法和用于此的设备。这些方法的实施例基于调节第一液化流的温度(Tx),以改变来自终端气/液分离器的终端气态流的量;和控制进给到富含甲烷的上部流中的终端压缩流的再循环馏分的量。
这样允许在第一和第二冷却剂回路之间变换压缩功率,并且提高第一和第二冷却剂回路两者的压缩功率(优选达满载),以产生更多的液化的烃产品流。因而,Tx的调节和再循环馏分的量的控制可允许在主冷却剂压缩机和第一冷却剂压缩机的最大负载下驱动主冷却剂压缩机和第一冷却剂压缩机中的每一个。
由于第一液化流的温度调节,代替提高压缩功率或除了提高压缩功率之外,根据本发明的方法和设备还可用于允许控制生产的液化的烃产品流的规格,有时称为质量。
有利地,本发明的实施例提供了使用NGL回收来液化烃流的方法,以改进C2+烃类从烃流分离,并且还提供了终端压缩流返回到液化过程的更有效的位置。
参照附图,图1显示了根据一个实施例的用于液化烃流的设备。该设备包括:
-NGL回收系统12,用于从烃进料流10提取C2+流,以提供至少富含甲烷的上部流20和富含C2+的下部流30;
-至少一第一压缩机24,用于从富含甲烷的上部流20形成压缩甲烷的流40;
-主冷却级42,用于液化富含甲烷的压缩流40,以形成第一液化流50;
-减压装置52,用于减小第一液化流50的压力,以形成混合相流60;
-终端气/液分离器62,用于将混合相流分离为终端气态流70和液化的烃产品流80;
-一个或多个终端压缩机72,用于压缩终端气态流70,以形成终端压缩流90;和
-再循环馏分管路90b,将终端压缩流90与富含甲烷的上部流20连接在一起,以将至少终端压缩上部流90的再循环馏分进给到富含甲烷的上部流20。
图1可还用于示出根据一个实施例的液化烃流的方法。该方法至少包括以下步骤:
-提供烃进料流10;
-将烃进料流10传送经过NGL回收系统12,以将烃进料流10分离为至少富含甲烷的上部流20和富含C2+的下部流30;
-将富含甲烷的上部流20传送经过至少一第一压缩机24,以形成压缩甲烷的流40;
-将压缩甲烷的流40液化,以形成第一液化流50;
-减小第一液化流50的压力,以形成混合相流60;
-将混合相流60传送经过终端气/液分离器62,以形成终端气态流70和液化的烃产品流80;
-将终端气态流70传送经过一个或多个终端压缩机72,以形成终端压缩流90;和
-将终端压缩流72的至少再循环馏分90b进给到富含甲烷的上部流20中。
烃流可以是任何合适的烃流,例如但是不限于能够被冷却的含烃气流。一个示例是从天然气或油藏获得的天然气流。作为替代,天然气流也可从另一种源获得,还包括合成源,例如费托工艺。
通常这样的烃流主要包括甲烷。优选地,这样的烃流包括至少50mol%甲烷,更优选地包括至少80mol%甲烷。
虽然本文所公开的方法可适用于多种烃流,但是其特别适用于待液化的天然气流。由于本领域技术人员易于理解怎样液化烃流,因此本文对此不详细讨论。
根据所述源的情况而定,烃流可包含一种或多种非烃类,例如H20,N2,CO2,Hg,H2S和其他硫化合物。
如果需要,烃流可在使用之前作为烃冷却工艺的一部分进行预处理,或单独进行预处理。该预处理可包括减少和/或去除非烃类,例如CO2和H2S,或可包括其他步骤,例如早期冷却和预加压。由于这些步骤为本领域技术人员众所周知,在此不对它们的机理进行进一步讨论。
因而,本文所用的术语“烃流”还包括在任何处理之前的组成,这样的处理包括清洁、脱水和/或洗涤,以及包括已经部分、基本上或全部处理以减少和/或去除一种或多种化合物或物质(包括但不限于硫、硫化合物、二氧化碳和水)的任何组成。
优选地,本文所用的烃流至少经受随后允许烃流液化所需的最少的预处理。将天然气液化所需的预处理是本领域已知的。
烃流通常还包含比甲烷更重的不同含量的烃类,例如乙烷、丙烷、丁烷和戊烷,以及一些芳香烃。组成根据烃流的类型和位置改变。由于若干原因,例如具有不同的凝固温度或液化温度,而这可能造成其将甲烷液化设备的部件阻塞,因此比甲烷更重的烃类通常需要从待液化的天然气去除。C2-4烃可用作天然气液体(NGLs)源和/或冷却剂。
液化工艺(其按常规在40到70巴的压力下进行)中使用的在高压下运行的洗涤塔可用于从烃流去除C5+烃,例如提供具有小于0.1mol%的C5+烃的经洗涤的流。
但是,甲烷和NGLs的在例如洗涤塔中的高压分离不像在低压下进行分离工艺那样有效,但是为了避免膨胀和然后再压缩主烃流所需的CAPEX和OPEX,按照常规保持高压是有利的。
因此,在一些情况下,洗涤塔可以不提供所需的LNG规格。例如,美国要求的LNG规格应包括不超过1.35mol%的C4+,不超过3.25mol%的丙烷,和不超过9.2mol%的乙烷。提供这样的规格的一种方法是在低压下,例如在15巴到45巴范围内,更优选地在20巴到35巴范围内进行NGLs分离。例如,C3+烃从烃流分离优选在30巴到35巴的压力范围内,更优选在33巴下进行,而C2+烃的分离优选在20巴到25巴的更低的压力范围内,更优选在23巴下进行。在在这些压力下进行NGL提取之后,烃流于是必须在液化之前进一步压缩。图1显示了根据本文公开的一个实施例的液化烃流的方法,其中,烃进料流10被传送到NGL回收系统12中。
烃进料流10从如上限定的烃流提供,并且在NGL回收系统12之前可经受一种或多种进一步的工艺或处理。例如,烃进料流10可通过如后文所讨论的一个或多个换热器冷却。
烃进料流10可以作为准备传送到为NGL回收系统12一部分的NGL回收塔14(图2中所示)中的低压混合相进料流提供。
替代地和/或另外,NGL回收系统12可包括至少一第一膨胀器15(图2中所示),其能够使烃进料流10膨胀,以形成用于NGL回收塔14的混合相进料流16。
NGL回收系统12以本领域已知的方式提供富含甲烷的上部流20和富含C2+的下部流30。通过在低压下操作,例如在≤35巴下操作,NGL回收系统12的NGL回收塔14提供比常规洗涤塔更有效的甲烷和C2+烃的分离。
富含C2+的下部流30可传送到可任选的分馏系统(未显示),该分馏系统包括一个或多个分离器,例如一个或多个蒸馏塔或分馏塔,以提供单独的烃流,例如乙烷流、丙烷流和丁烷流,或其组合,用于单独使用或至少部分用作本文所公开的液化烃流方法的一种或多种冷却剂的一种或多种组分。
富含甲烷的上部流20可仍包括微少量(<10mol%)的C2+烃,和优选>80mol%,更优选>90mol%的甲烷和氮气。
富含甲烷的上部流20被传送经过第一压缩机24,以形成压缩甲烷的流40。第一压缩机24可以按本领域已知的方式包括一个或多个压缩机、级和/或段,并且用于提供压力在30到80巴范围内,优选从35巴或40巴到80巴,更优选从45巴到80巴压力的压缩甲烷的流40。该压力或该压力范围的下限可根据富含甲烷的上部流20从NLG回收系统排出时具有的压力选择。
然后将压缩甲烷的流40液化,以形成第一液化流50。压缩甲烷的流40的液化可通过包括一个或多个换热器的一个或多个冷却级进行,其中,压缩甲烷的流可与蒸发的冷却剂进行热交换。图1以举例的方式显示了能够将压缩甲烷的流40冷却到至少-100℃的温度的“主”冷却级42。
主冷却级42可包括一个或多个主冷却剂回路。至少一个主冷却剂回路可包括混合冷却剂,该混合冷却剂包括包含氮气、甲烷、乙烷、乙烯、丙烷、丙烯、丁烷和戊烷的组中的两种或更多种。在主冷却级42中进行该液化之前,烃进料流10和/或压缩甲烷的流40可通过包括一个或多个第一冷却剂回路压缩机的一个或多个第一冷却剂回路冷却。第一冷却剂回路的冷却剂可主要包括包含氮气、甲烷、乙烷、乙烯、丙烷、丙烯、丁烷和戊烷的组中的一种或多种。
然后将第一液化流50的压力减小,以形成混合相流60。液化流的压力的减小可通过本领域已知的任何适当的设备、单元或装置进行,例如膨胀装置,例如一个或多个阀和/或一个或多个膨胀器。图1显示了使用阀52的示例。
然后将混合相流60传送到终端气/液分离器62中,例如传送到本领域已知的终端闪蒸容器中,其中,在那里形成液化的烃产品流80和终端气态流70,例如终端闪蒸气流。液化的烃产品流80的压力和/或终端气态流70的压力可接近大气压,例如小于1.5巴。
液化的烃产品流80可然后通过一个或多个泵(未显示)传送到存储和/或运输设备。在烃进料流10为天然气的情况下,液化的烃产品流80为LNG。
然后来自终端气/液分离器62的终端气态流70例如终端闪蒸气体传送经过一个或多个终端压缩机72,以形成终端压缩流90。一个或多个终端压缩机72可以是本领域已知的具有一级或多级和/或一段或多段的任何合适的压缩机,并且用于形成压力>20巴的终端压缩流90。
终端压缩流90由本领域已知的流分流器91分离,以形成再循环馏分90b和燃料气体馏分90a。终端压缩流90也可用于一种或多种其他用途,例如给一个或多个换热器提供冷却,并且可提供一种或多种用于除了再循环和燃料流之外的其他馏分。终端压缩流90的其他用途在本领域是已知的。
由流分流器91对终端压缩流90的分离可根据如下讨论的对再循环馏分90b的需要在0-100%范围内的任何位置处进行。
方便地,再循环馏分90b处于与富含甲烷的上部流20相同或相似的压力下,以使得其可能通过第一压缩机24上游的组合器21容易地进给到富含甲烷的上部流20中。
图2显示了根据本文公开的第二实施例的液化烃流的方法。
图2中,烃进料流10在传送到NGL回收系统12中之前,传送经过第一换热器110、第二换热器112和第三换热器114,所述第二换热器112优选为低压釜式(kettle)换热器。以这种方式,烃进料流10的温度可降到低于0℃。压力可以是在40巴到80巴范围内,优选在45巴到80巴范围内的任何压力。
图2中,NGL回收系统12包括预NGL分离器17,其能够形成下部液流18,该下部液流18传送经过阀13,并且传送到NGL回收塔14中;并且能够形成上部气态流19,该上部气态流19传送到NGL膨胀器15中,以形成混合相进料流16,该混合相进料流16在高于下部液流18的高度处传送到NGL回收塔14中。
NGL回收塔14形成富含C2+的下部流30,和上部流31,该上部流31传送经过第一和第三换热器110,114,以提供对烃进料流10的一些冷却。之后,上部流31可传送通过涡轮压缩机32,其优选以机械方式与NGL膨胀器15相互连接,并且由NGL膨胀器15直接驱动,以获取由NGL膨胀器以本领域已知的方式产生的作用能。涡轮压缩机形成富含甲烷的上部流20,该富含甲烷的上部流20从NGL回收系统12提供。
如上所述,富含甲烷的上部流20可由组合器21与终端压缩流90的再循环馏分90b混合,以将进料流供给到一个或多个第一压缩机24中。可任选地,中间冷却器25可与一个或多个第一压缩机24一起设置。形成的压缩甲烷的流40可由第一冷却器26冷却。中间冷却器25和第一冷却器26可以是本领域已知的水和/或空气冷却器。压缩甲烷的流40可传送经过第四换热器或换热器系统116,该第四换热器或换热器系统116优选为高压釜式换热器116a、中压换热器116b和低压换热器116c,其中,压缩甲烷的流40可与在上面指出的多个相对压力水平下蒸发的冷却剂换热,以在进入主冷却级42之前形成冷却的压缩甲烷的流40a。
根据本文公开的一个实施例,设置第一冷却剂回路100,其包括由第一冷却剂压缩机驱动器D2驱动的第一冷却剂压缩机101(为一个或多个压缩机),该第一冷却剂压缩机101提供加压的冷却剂流108。加压的冷却剂流108传送经过一个或多个冷却器102和阀103,以将冷却的膨胀的冷却剂流104供给到一个或多个换热器中。图2仅以举例的方式显示了第一冷却剂回路100,其将冷却剂供给分流到两个平行的第一高压(HP)釜式换热器105a,105b。然后第一高压换热器105a,105b中的每一个经由膨胀装置(未显示)将冷却剂传送到中压(MP)釜式换热器106a,106b。来自中压釜式换热器106a的冷却剂供给到低压(LP)釜式换热器107a。在图2中所示的实施例中,来自中压(MP)釜式换热器106b的冷却剂被分流,以供给两个低压换热器107b,107c。可任选地,低压换热器107c可对应于第二换热器112,用于冷却烃进料流10。然后将来自低压釜式换热器107a,107b,112的冷却剂通过第一冷却剂压缩机101再压缩。
还可任选地,HP换热器105a,105b中的一个可对应于第四HP换热器116a,第四HP换热器116a能够在第一压缩机14之后给压缩甲烷的流40提供冷却。类似地,MP换热器106a,106b中的一个可对应于第四MP换热器116b,并且LP换热器107a,107b中的一个可对应于第四LP换热器116c。
在用于液化烃流的工艺中设置第一冷却剂回路在本领域中是已知的,并且有时称为“预冷却冷却剂回路”。第一冷却剂回路可还对一种或多种其他流提供一些冷却,所述其他流包括烃液化工艺中一个或多个其他冷却剂回路中的冷却剂,例如主冷却剂回路中的主冷却剂。
第一冷却剂回路中的第一冷却剂可以是单组份冷却剂,例如主要包含丙烷或丙烯,优选为丙烷,或可以是包含一种或多种组分的冷却剂,所述一种或多种组分选自包括氮气、甲烷、乙烷、乙烯、丙烷、丙烯、丁烷和戊烷的组。
第一压缩机24可由专用驱动器D1(例如图1中标示的)驱动。但是,第一冷却剂压缩机101的第一冷却剂压缩机驱动器D2也可驱动第一压缩机24。例如,在图2中所示的实施例中,第一压缩机24和至少一个冷却剂压缩机101以机械方式相互连接,并且通常通过使用共用的驱动轴27被共同地驱动。这样的共同驱动方案的优点是,来自第一冷却剂回路的过多的可用功率因而可不仅用于给第一冷却剂提供更多的冷却任务(这是提高产量所需的),而且可用于再压缩由于较高的温度Tx产生的另外的再循环气体。
来自第四换热器系统116的冷却的压缩甲烷的流40a传送到主冷却级42中。第四换热器系统可包括一个或多个第四高压釜式换热器116a、一个或多个第四中压换热器116b和一个或多个第四低压换热器116c。图2中仅分别显示了一个第四HP、MP和LP釜式换热器116a,116b,116c。
主冷却级42可包括串联、并联或串联并联都存在的一个或多个换热器和一个或多个冷却剂回路。图2显示了主冷却级42具有主低温换热器(MCHE)54,例如缠绕管式换热器,其能够通过与主冷却剂热交换而冷却并且至少部分液化冷却的压缩甲烷的流40a,以形成第一液流50。
图2还显示了主冷却级42具有主冷却回路44,该主冷却回路44可使用任何冷却剂,优选为包括包含氮气、甲烷、乙烷、乙烯、丙烷、丙烯、丁烷、戊烷的组中的两种或更多种的混合冷却剂。
主冷却剂回路44可包含任意数量的冷却剂压缩机、冷却器和分离器,用于以本领域已知的方式向MCHE 54提供一个或多个冷却剂流。
图2仅以举例的方式显示了主冷却剂回路44具有第一和第二主冷却剂压缩机45a,45b,所述第一和第二主冷却剂压缩机45a,45b共同由主冷却剂压缩机驱动器D3驱动,以形成传送经过一个或多个冷却器47的加压的冷却剂流46,所述一个或多个冷却器47例如为一个或多个水和/或空气冷却器,其后为第五换热器系统118,第五换热器系统118包括一个或多个第五HP釜式换热器118a、一个或多个第五MP釜式换热器118b和一个或多个LP釜式换热器118c。图2中仅显示了一个第五HP、MP和LP釜式换热器118a,118b,118c。第五HP、MP和LP釜式换热器118a,118b,118c可对应于第一冷却剂回路100中的第一HP、MP和LP换热器105a,105b,106a,106b,107a,107b,107c中的一个或多个。因而形成冷却的,优选部分冷凝并且加压的冷却剂流48,其被传送到冷却剂分离器55。冷却剂分离器55适于以本领域已知的方式提供轻冷却剂流56和重冷却剂流57,所述冷却剂流56,57传送经过MCHE 54,以进一步冷却形成低温冷却的冷凝冷却剂流,其在重新进入MCHE 54来在其中提供冷却之前,由一个或多个阀和/或膨胀器58a,58b膨胀。MCHE 54形成温的冷却剂流59,以在第一和第二冷却剂压缩机45a,45b中再压缩。第二主冷却剂压缩机45b可装配有一个或多个中间冷却器43,例如一个或多个水和/或空气冷却器。
如上所述,来自MCHE 54的第一液化流50传送经过减压装置,例如阀52,进入终端气-液分离器62,例如终端闪蒸容器,以形成终端气态流70,例如终端闪蒸气体,和液化的烃产品流80。替代地,减压装置可以是膨胀器或阀和膨胀器的组合。终端气态流70传送经过由终端压缩机驱动器D4驱动的图2中所示的一个或多个终端压缩机72,以形成终端压缩流90。终端压缩流90的再循环馏分90b由分流器91提供,以进给到富含甲烷的流20中。
图3显示了根据第三实施例的液化烃流的方法的替代布置。图3使用与图2中所述的实施例相同的装置,但是由第一冷却剂回路100提供的冷却采用不同的布置。
图3显示了烃进料流10传送经过NGL回收系统12,以形成富含甲烷的上部流20,该富含甲烷的上部流20经过至少一第一压缩机24,以形成压缩甲烷的流40。图3显示了第一冷却剂回路100包括由第一冷却剂压缩机驱动器D2驱动的第一冷却剂压缩机101,和一个或多个冷却器102及其后的阀103。
图3示出了换热系统120,作为对通过第一冷却剂回路100给该液化方法中的其他流提供冷却的示意性图示。换热系统120的虚线方块122代表一个或多个实际的换热器,例如釜式,第一冷却剂回路100的第一冷却剂可传送经过所述换热器来给所示的传送经过换热系统120的其他流提供冷却。
第一冷却剂回路100以图2中第四换热器系统116的方式给压缩甲烷的流40提供冷却,从而形成冷却的压缩甲烷的流40a,并且以图2中所示的第五换热器系统118的方式给主冷却剂回路44的主冷却剂提供冷却(在其传送经过由主冷却剂压缩机驱动器D3驱动的一个或多个主压缩机45,和一个或多个冷却器47,以形成冷却的加压冷却剂流48之后)。在换热系统120中对冷却的加压冷却剂流48的冷却形成进一步冷却的加压的冷却剂流49,该冷却剂流49传送到阀41,然后传送到主冷却级42。
管路124代表可由换热系统120冷却的其他流,以形成冷却的其他流124a。这样的冷却可例如以与图2中所示的与第二换热器112相关的方式提供给通过管路126和126a的烃进料流10。
图3显示在冷却的压缩甲烷的流40a传送经过主冷却级阶段42之后,形成了温度为Tx的第一液化流50。
本文公开的实施例提供了液化烃流的有利方法,其中,终端压缩流90的压力与在NGL回收之后的富含甲烷的上部流20的压力相同或相似,以使至少终端压缩流90的至少一部分可能直接再循环回到该液化工艺中。
本文公开的实施例还提供了控制烃进料流10液化的方法,包括以下步骤:
(i)如上所述将烃进料流10液化;
(ii)调节图3中所示的第一液化流50的温度Tx,以改变来自终端气/液分离器62的终端气态流70的量;和
(iii)控制作为再循环馏分进给到富含甲烷的流20中的终端压缩流90的再循环馏分90b的量。
调节第一液化流50的温度Tx允许有利地调节和/或变换液化工艺中所用的压缩机的驱动器中的一个或多个的功率要求。
例如,将第一液化流50的温度Tx升高几摄氏度,例如从-144.5℃升高到-140℃或-130℃,就增加了终端气/液分离器62中提供的终端气态流70,从而需要来自终端压缩机驱动器D4的更多的功率以压缩增加的终端气态流70,并且因此用于同样的再循环馏分90b体积的第一压缩机驱动器D1和第一冷却剂压缩机驱动器D2需要更多的功率。但是主冷却剂压缩机驱动器D3需要更少的功率(因为主冷却级42中的液化温度更高)。
相反地,降低温度Tx就减少了提供的终端气态流70,减小了压缩机驱动器D4、D1和D2的功率负载(用于相同的再循环馏分90b体积),但是增加了主冷却剂压缩机D3功率负载(以降低液化温度)。
图2和3中所示的压缩机驱动器D1-4的功率负载可进一步通过控制再循环馏分90b和燃料馏分90a的量来改变。一个或多个用户对燃料馏分90a的需求可能会改变,这决定再循环馏分90b的量。
图3显示了四个压缩机驱动器D1-4和终端流分流器91之间的相互关系,这使得能够理解其间的改变。
以这种方式,本文提供的控制烃进料流10液化的方法允许用户通过在用于给定烃进料流的压缩机驱动器之间变换功率负载来控制液化工艺。
例如,在一个或多个压缩机驱动器被抑制的情况下,即已经满载,并且不能给流经的流提供任何进一步的压缩,则可通过改变最终液化流50的温度Tx和控制再循环馏分90a的量来改变一个或多个其他压缩机驱动器来适应,并且如果需要,缓解受抑制的驱动器。通常,受抑制的第一冷却剂压缩机驱动器D2或主冷却剂压缩机驱动器D3在液化工艺中是较大的驱动器。
本文公开的实施例还提供最大化液化烃流80产量的方法,包括至少以下步骤:
-如上所述控制烃进料流10的液化,包括主冷却剂回路44、一个或多个主冷却剂压缩机45、第一冷却剂回路100和一个或多个第一冷却剂压缩机101;和
-将一个或多个主冷却剂压缩机45和第一冷却剂压缩机101中的每一个在其最大负载下驱动。
以这种方式,可通过使所有冷却剂驱动器D1-4满载来提高液化烃流的产量,否则的话,一个或多个所述驱动器可能不需要满载。
例如,驱动器D1-4中的一个或多个,特别是第一冷却剂驱动器D2和主冷却剂压缩机驱动器D3可具有多余的容量,同时,相对于其他压缩机驱动器,仍能够提供期望或“正常”量的液化烃产品。
液化的烃流可以是液化的天然气流。
在目前公开的实施例中,控制第一液化流50的温度Tx和终端压缩流90的再循环馏分90的量允许至少将第一冷却剂压缩机驱动器D2和主冷却剂压缩机驱动器D3最大化到全功率,以增加液化烃产品流80。
下面的表1提供了与涉及无终端压缩流的再循环(即无再循环馏分90b)的工艺相比较,本文公开的工艺的一个示例(例如图2和3种所示)的各部分处驱动器和一些流的功率负载和其他数据。
表1
流/驱动器 | 单位 | 不具有再循环 | 具有再循环 |
D1 | MW | 17.52 | 30.09 |
D2 | MW | 89.20 | 90.19 |
D3 | MW | 178.40 | 180.29 |
D4 | MW | 68.79 | 77.75 |
80 | MTPA | 7.50 | 8.00 |
70 | kg/s | 23.03 | 41.11 |
90b | kg/s | 0.00 | 18.92 |
第一压缩机24的压力 | 巴 | 25.15 | 25.15 |
温度Tx | ℃ | -149.9 | -144.5 |
表1证明,在第一冷却剂压缩机驱动器D2和主冷却剂压缩机驱动器D3提供相似的功率的情况下,通过使用终端气态流的再循环馏分90b和通过满载使用其他压缩驱动器D1和D4中可用的功率,可提供约7%的流80(例如LNG)产量的增加。
表1显示了示例和比较例(即具有和不具有再循环的工艺),其中,第一冷却剂压缩机驱动器D2和主冷却剂驱动器D3在对应于其安装的功率输出的满载下运行。在不具有再循环的比较例中,第一压缩机驱动器D1和终端压缩机驱动器D4在明显低于其相应的安装功率的耗用功率水平下运行。仅在具有再循环的示例中,驱动器D1和D4可在近似其安装功率的耗用功率水平下运行。
图4显示了控制系统200可怎样结合到上述用于液化烃流的方法和设备中的示例。该图显示了如本文上面的描述布置的NGL回收系统12、第一压缩机24及其驱动器D1、第一冷却剂回路100、主冷却剂回路42、减压装置52、终端气/液分离器62、终端压缩机72和再循环馏分管路90b。该示例中减压装置52以后面为流动控制阀53的膨胀器51的形式实现,流动控制阀53布置在膨胀器52下游的管路60中。控制系统200包括控制器C,其布置用于通过调节第一液化流50的温度Tx来改变来自终端气/液分离器62的终端气态流70的量和通过控制再循环馏分管路90b中的量,而将主冷却剂回路42中的一个或多个主冷却剂压缩机和第一冷却剂回路100中的一个或多个第一冷却剂压缩机的负载功率最大化到其最大负载。温度Tx可通过以下方式来调节:通过计算并施加新设置点温度Tx’,并且通过操纵流动控制阀53来布置控制系统以尽可能接近地将温度Tx保持到设置点温度Tx’。再循环馏分90b中的量也根据设置点使用流F来进行流动控制。该流设置点通过控制器C转换为对再循环控制阀201的设置。因而,第一和主冷却剂压缩机的功率负载可在控制系统200中实现为受控制变量,并且流动控制阀52和再循环控制阀201的控制阀设置可视为受操纵变量。
本领域技术人员将理解,本发明可按多种方式实现而不偏离本发明请求保护的范围。
Claims (16)
1.一种液化烃流的方法,包括至少以下步骤:
(a)提供液化系统,其包括至少NGL回收系统、主冷却剂回路和第一冷却剂回路以及减压装置,减压装置之后为气/液分离器,所述主冷却剂回路包括至少一个或多个主冷却剂压缩机,并且所述第一冷却剂回路包括一个或多个第一冷却剂压缩机;
(b)将烃进料流传送经过所述NGL回收系统,以从所述烃进料流产生富含甲烷的上部流;
(c)将所述富含甲烷的上部流传送经过至少一第一压缩机,以形成压缩甲烷的流;
(d)借助于所述第一冷却剂回路中的第一冷却剂冷却所述压缩甲烷的流,随后借助于所述主冷却剂回路中的主冷却剂液化所述压缩甲烷的流,以形成第一液化流;
(e)减小所述第一液化流的压力,以形成混合相流;
(f)将所述混合相流传送经过终端气/液分离器,以形成终端气态流和液化的烃产品流;
(g)将所述终端气态流的至少再循环馏分进给到所述富含甲烷的上部流中或进给到在借助于所述第一冷却剂回路中的所述第一冷却剂进行的所述冷却的至少一部分上游的甲烷压缩流中;
(h)通过调节第一液化流的温度(Tx)来改变来自终端气/液分离器的终端气态流的量和控制步骤(g)中进给的终端气态流的再循环馏分的量,而将所述一个或多个主冷却剂压缩机和所述一个或多个第一冷却剂压缩机的负载功率最大化到其最大负载。
2.根据权利要求1所述的方法,其中,在步骤(b)中产生富含甲烷的上部流包括从烃进料流提取C2+流和形成富含C2+的下部流。
3.根据权利要求1或权利要求2所述的方法,其中,所述NGL回收系统包括膨胀器、NGL回收塔和一个或多个与所述膨胀器以机械方式相互连接以由所述膨胀器驱动的涡轮压缩机,并且其中,步骤(b)包括将烃进料流的至少一部分传送经过所述膨胀器,以形成混合相进料流;将所述混合相进料流传送到所述NGL回收塔中,产生上部流,并且将所述上部流传送经过所述涡轮压缩机,以产生富含甲烷的上部流。
4.根据权利要求3所述的方法,其中,所述NGL回收塔中的压力小于40巴,更优选≤35巴。
5.根据权利要求3所述的方法,其中,所述NGL回收塔中的压力在从15巴到45巴的范围内,优选在从20巴到35巴的范围内。
6.根据权利要求1到5中任一项所述的方法,其中,所述第一冷却剂回路包括用于冷却烃进料流的至少一个换热器,和用于冷却压缩甲烷的流的至少一个换热器。
7.根据权利要求1到6中任一项所述的方法,还包括将所述终端气态流传送经过一个或多个终端压缩机,以在步骤(g)之前形成终端压缩流,并且其中,所述终端气态流的再循环馏分从所述终端压缩流提取。
8.根据权利要求1到7中任一项所述的方法,其中,所述富含甲烷的上部流的压力和所述终端压缩流的再循环馏分的压力在15巴到45巴的范围内。
9.根据权利要求1到8中任一项所述的方法,其中,所述第一压缩机与至少一个所述第一冷却剂压缩机被共同地驱动。
10.根据权利要求1到9中任一项所述的方法,其中,所述烃进料流为天然气流,并且所述液化的烃产品流为液化的天然气流。
11.根据权利要求1到10中任一项所述的方法,其中,步骤(h)中对第一液化流的温度(Tx)的调节和对步骤(g)中进给的所述终端气态流的再循环馏分的量的控制提高了所述液化的烃产品流的产量,优选使得所述液化的烃产品流的产量最大化。
12.根据权利要求1到11中任一项所述的方法,其中,步骤(h)中负载功率的最大化包括在所述第一冷却剂压缩机和所述主冷却剂压缩机之间变换功率负载。
13.一种用于液化烃流的设备,所述设备至少包括:
-NGL回收系统,用于从烃进料流提取C2+气流,以至少形成富含甲烷的上部流和富含C2+的下部流;
-至少一第一压缩机,用于从所述富含甲烷的上部流形成压缩甲烷的流;
-第一冷却级,用于冷却所述压缩甲烷的流,以形成冷却的压缩甲烷的流,随后为主冷却级,用于液化所述冷却的压缩甲烷的流,以形成第一液化流,其中,所述第一冷却级包括第一冷却剂回路,所述第一冷却剂回路包括一个或多个第一冷却剂压缩机,并且其中,所述主冷却级包括主冷却剂回路,所述主冷却剂回路包括一个或多个主冷却剂压缩机;
-减压装置,用于减小所述第一液化流的压力,以形成混合相流;
-终端气/液分离器,用于将所述混合相流分离为终端气态流和液化的烃产品流;
-再循环馏分管路,用于将所述终端气态流的至少再循环馏分进给到所述富含甲烷的上部流中;和
-控制系统,布置用于通过调节所述第一液化流的温度(Tx)来改变来自所述终端气/液分离器的所述终端气态流的量和控制所述再循环馏分管路中所述终端压缩流的再循环馏分的量,而将所述一个或多个主冷却剂压缩机和所述一个或多个第一冷却剂压缩机的负载功率最大化到其最大负载。
14.根据权利要求13所述的设备,其中,所述NGL回收系统包括:
-膨胀器,布置用于将至少一部分烃进料流膨胀,以形成混合相进料流;
-NGL回收塔,用于接收所述混合相进料流,并且用于产生上部流;和
-一个或多个涡轮压缩机,以机械方式与所述膨胀器相互连接以由所述膨胀器驱动,用于接收所述上部流并且产生所述富含甲烷的上部流。
15.根据权利要求13或14所述的设备,还包括一个或多个终端压缩机,用于压缩所述终端气态流,以形成终端压缩流,其中,所述再循环馏分管路将所述终端压缩流与所述富含甲烷的上部流连接。
16.根据权利要求13到15中任一项所述的设备,其中,所述一个或多个第一压缩机中的至少一个和所述第一压缩机以机械方式相互连接并且被共同地驱动。
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US12/100,287 US8534094B2 (en) | 2008-04-09 | 2008-04-09 | Method and apparatus for liquefying a hydrocarbon stream |
US12/100,287 | 2008-04-09 | ||
PCT/EP2009/054125 WO2009124925A2 (en) | 2008-04-09 | 2009-04-07 | Method and apparatus for liquefying a hydrocarbon stream |
Publications (1)
Publication Number | Publication Date |
---|---|
CN102762944A true CN102762944A (zh) | 2012-10-31 |
Family
ID=41162295
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN2009801114011A Pending CN102762944A (zh) | 2008-04-09 | 2009-04-07 | 用于液化烃流的方法和设备 |
Country Status (7)
Country | Link |
---|---|
US (2) | US8534094B2 (zh) |
EP (1) | EP2422151A2 (zh) |
JP (1) | JP5325284B2 (zh) |
CN (1) | CN102762944A (zh) |
AU (1) | AU2009235461B2 (zh) |
RU (1) | RU2499209C2 (zh) |
WO (1) | WO2009124925A2 (zh) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105143800A (zh) * | 2012-11-02 | 2015-12-09 | 林德股份公司 | 用于冷却富烃馏分的方法 |
CN107110599A (zh) * | 2015-01-09 | 2017-08-29 | 三菱重工业株式会社 | 气体液化装置以及气体液化方法 |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2469077A (en) * | 2009-03-31 | 2010-10-06 | Dps Bristol | Process for the offshore liquefaction of a natural gas feed |
US20150153100A1 (en) * | 2013-12-04 | 2015-06-04 | General Electric Company | System and method for hybrid refrigeration gas liquefaction |
TWI707115B (zh) * | 2015-04-10 | 2020-10-11 | 美商圖表能源與化學有限公司 | 混合製冷劑液化系統和方法 |
GB2539955A (en) * | 2015-07-03 | 2017-01-04 | Frederick Skinner Geoffrey | Process for producing liquefied natural gas |
US20170097188A1 (en) * | 2015-10-06 | 2017-04-06 | Sorin T. Lupascu | Consolidated Refrigeration And Liquefaction Module In A Hydrocarbon Processing Plant |
US20170198966A1 (en) * | 2016-01-11 | 2017-07-13 | GE Oil & Gas, Inc. | Reducing refrigeration duty on a refrigeration unit in a gas processing system |
KR101792708B1 (ko) * | 2016-06-22 | 2017-11-02 | 삼성중공업(주) | 유체냉각장치 |
FR3053770B1 (fr) * | 2016-07-06 | 2019-07-19 | Saipem S.P.A. | Procede de liquefaction de gaz naturel et de recuperation d'eventuels liquides du gaz naturel comprenant un cycle refrigerant semi-ouvert au gaz naturel et deux cycles refrigerant fermes au gaz refrigerant |
US10753677B2 (en) | 2017-06-08 | 2020-08-25 | General Electric Company | Methods and systems for enhancing production of liquefied natural gas |
US10753676B2 (en) | 2017-09-28 | 2020-08-25 | Air Products And Chemicals, Inc. | Multiple pressure mixed refrigerant cooling process |
US10852059B2 (en) | 2017-09-28 | 2020-12-01 | Air Products And Chemicals, Inc. | Multiple pressure mixed refrigerant cooling system |
US11499775B2 (en) | 2020-06-30 | 2022-11-15 | Air Products And Chemicals, Inc. | Liquefaction system |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4541852A (en) * | 1984-02-13 | 1985-09-17 | Air Products And Chemicals, Inc. | Deep flash LNG cycle |
US5669234A (en) * | 1996-07-16 | 1997-09-23 | Phillips Petroleum Company | Efficiency improvement of open-cycle cascaded refrigeration process |
CN1135350C (zh) * | 1997-12-12 | 2004-01-21 | 国际壳牌研究有限公司 | 制取液化天然气的气态富甲烷给料的液化方法 |
US20070157663A1 (en) * | 2005-07-07 | 2007-07-12 | Fluor Technologies Corporation | Configurations and methods of integrated NGL recovery and LNG liquefaction |
WO2007135062A2 (en) * | 2006-05-19 | 2007-11-29 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for treating a hydrocarbon stream |
Family Cites Families (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3983711A (en) * | 1975-01-02 | 1976-10-05 | The Lummus Company | Plural stage distillation of a natural gas stream |
US4445916A (en) * | 1982-08-30 | 1984-05-01 | Newton Charles L | Process for liquefying methane |
SU1354007A1 (ru) * | 1985-11-18 | 1987-11-23 | Предприятие П/Я Р-6956 | Способ управлени установкой сжижени природного газа |
US5036671A (en) * | 1990-02-06 | 1991-08-06 | Liquid Air Engineering Company | Method of liquefying natural gas |
US5662934A (en) * | 1993-01-05 | 1997-09-02 | Najarian; Thomas | Compositions and methods for lowering cholesterol while maintaining antioxidant levels |
US5615561A (en) * | 1994-11-08 | 1997-04-01 | Williams Field Services Company | LNG production in cryogenic natural gas processing plants |
TW366411B (en) * | 1997-06-20 | 1999-08-11 | Exxon Production Research Co | Improved process for liquefaction of natural gas |
US5791160A (en) * | 1997-07-24 | 1998-08-11 | Air Products And Chemicals, Inc. | Method and apparatus for regulatory control of production and temperature in a mixed refrigerant liquefied natural gas facility |
US6041620A (en) * | 1998-12-30 | 2000-03-28 | Praxair Technology, Inc. | Cryogenic industrial gas liquefaction with hybrid refrigeration generation |
WO2001088447A1 (en) | 2000-05-18 | 2001-11-22 | Phillips Petroleum Company | Enhanced ngl recovery utilizing refrigeration and reflux from lng plants |
US6712880B2 (en) * | 2001-03-01 | 2004-03-30 | Abb Lummus Global, Inc. | Cryogenic process utilizing high pressure absorber column |
US6427483B1 (en) * | 2001-11-09 | 2002-08-06 | Praxair Technology, Inc. | Cryogenic industrial gas refrigeration system |
US6889523B2 (en) * | 2003-03-07 | 2005-05-10 | Elkcorp | LNG production in cryogenic natural gas processing plants |
FR2855526B1 (fr) * | 2003-06-02 | 2007-01-26 | Technip France | Procede et installation de production simultanee d'un gaz naturel apte a etre liquefie et d'une coupe de liquides du gaz naturel |
US7673476B2 (en) * | 2005-03-28 | 2010-03-09 | Cambridge Cryogenics Technologies | Compact, modular method and apparatus for liquefying natural gas |
EA014193B1 (ru) * | 2005-04-12 | 2010-10-29 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Способ ожижения потока природного газа |
US20070012072A1 (en) * | 2005-07-12 | 2007-01-18 | Wesley Qualls | Lng facility with integrated ngl extraction technology for enhanced ngl recovery and product flexibility |
WO2008017577A1 (de) * | 2006-08-07 | 2008-02-14 | Alstom Technology Ltd | Verfahren zur abtrennung von co2 aus einem gasstrom, co2-abtrennvorrichtung zur durchführung des verfahrens, dralldüse für eine co2-abtrennvorrichtung sowie anwendung der co2-abtrennvorrichtung |
-
2008
- 2008-04-09 US US12/100,287 patent/US8534094B2/en active Active
-
2009
- 2009-04-07 JP JP2011503419A patent/JP5325284B2/ja not_active Expired - Fee Related
- 2009-04-07 WO PCT/EP2009/054125 patent/WO2009124925A2/en active Application Filing
- 2009-04-07 EP EP09729348A patent/EP2422151A2/en not_active Withdrawn
- 2009-04-07 AU AU2009235461A patent/AU2009235461B2/en active Active
- 2009-04-07 US US12/936,601 patent/US9310127B2/en active Active
- 2009-04-07 RU RU2010145329/06A patent/RU2499209C2/ru active
- 2009-04-07 CN CN2009801114011A patent/CN102762944A/zh active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4541852A (en) * | 1984-02-13 | 1985-09-17 | Air Products And Chemicals, Inc. | Deep flash LNG cycle |
US5669234A (en) * | 1996-07-16 | 1997-09-23 | Phillips Petroleum Company | Efficiency improvement of open-cycle cascaded refrigeration process |
CN1135350C (zh) * | 1997-12-12 | 2004-01-21 | 国际壳牌研究有限公司 | 制取液化天然气的气态富甲烷给料的液化方法 |
US20070157663A1 (en) * | 2005-07-07 | 2007-07-12 | Fluor Technologies Corporation | Configurations and methods of integrated NGL recovery and LNG liquefaction |
WO2007135062A2 (en) * | 2006-05-19 | 2007-11-29 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for treating a hydrocarbon stream |
Non-Patent Citations (1)
Title |
---|
PIERRE RABEAU: "How to reduce CO2 emissions in the LNG chain", 《LNG15 INTERNATIONAL CONFERENCE》 * |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105143800A (zh) * | 2012-11-02 | 2015-12-09 | 林德股份公司 | 用于冷却富烃馏分的方法 |
CN105143800B (zh) * | 2012-11-02 | 2017-10-27 | 林德股份公司 | 用于冷却富烃馏分的方法 |
CN107110599A (zh) * | 2015-01-09 | 2017-08-29 | 三菱重工业株式会社 | 气体液化装置以及气体液化方法 |
CN107110599B (zh) * | 2015-01-09 | 2019-12-27 | 三菱重工工程株式会社 | 气体液化装置以及气体液化方法 |
Also Published As
Publication number | Publication date |
---|---|
RU2499209C2 (ru) | 2013-11-20 |
AU2009235461A1 (en) | 2009-10-15 |
WO2009124925A2 (en) | 2009-10-15 |
WO2009124925A3 (en) | 2012-11-22 |
US20110056237A1 (en) | 2011-03-10 |
JP5325284B2 (ja) | 2013-10-23 |
EP2422151A2 (en) | 2012-02-29 |
JP2011528424A (ja) | 2011-11-17 |
AU2009235461B2 (en) | 2012-04-26 |
US8534094B2 (en) | 2013-09-17 |
RU2010145329A (ru) | 2012-05-20 |
US9310127B2 (en) | 2016-04-12 |
US20090255294A1 (en) | 2009-10-15 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN102762944A (zh) | 用于液化烃流的方法和设备 | |
KR101393384B1 (ko) | 천연 가스 스트림의 액화 방법 및 장치 | |
CN100445673C (zh) | 用于液化高压天然气的系统和方法 | |
CN101156038B (zh) | 用于液化天然气流的方法和设备 | |
KR101568763B1 (ko) | Lng를 생산하는 방법 및 시스템 | |
JP4548867B2 (ja) | 天然ガスの改良液化方法 | |
CN104342220B (zh) | 氮去除和等压开放式制冷的天然气液回收 | |
US9759481B2 (en) | Method for producing a flow which is rich in methane and a cut which is rich in C2+ hydrocarbons from a flow of feed natural gas and an associated installation | |
CN100547326C (zh) | 精制天然气、富c3+烃馏分及富乙烷流束的生产方法和设备 | |
US3721099A (en) | Fractional condensation of natural gas | |
US9435583B2 (en) | Method and apparatus for liquefying a hydrocarbon stream | |
RU2436024C2 (ru) | Способ и устройство для обработки потока углеводородов | |
CN107917577B (zh) | 多压力混合的制冷剂冷却方法和系统 | |
JP2008530505A (ja) | 天然ガスを液化するためのプラント及び方法 | |
KR20120040700A (ko) | 다상 탄화수소 스트림을 처리하는 방법 및 이를 위한 장치 | |
US20200386090A1 (en) | Method to recover and process methane and condensates from flare gas systems | |
RU2423653C2 (ru) | Способ для сжижения потока углеводородов и установка для его осуществления | |
CN116783438A (zh) | 从初始天然气流中提取乙烷的方法和相应的设备 | |
CN115046366A (zh) | 一种回收天然气中乙烷的处理工艺 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
C06 | Publication | ||
PB01 | Publication | ||
C10 | Entry into substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
AD01 | Patent right deemed abandoned |
Effective date of abandoning: 20160413 |
|
C20 | Patent right or utility model deemed to be abandoned or is abandoned |