CN110537064A - Device and method for liquefied natural gas and the ship including the equipment - Google Patents
Device and method for liquefied natural gas and the ship including the equipment Download PDFInfo
- Publication number
- CN110537064A CN110537064A CN201780085095.3A CN201780085095A CN110537064A CN 110537064 A CN110537064 A CN 110537064A CN 201780085095 A CN201780085095 A CN 201780085095A CN 110537064 A CN110537064 A CN 110537064A
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- natural gas
- mixture
- cooling
- compound
- 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.)
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- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims description 44
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 212
- 239000000203 mixture Substances 0.000 claims abstract description 117
- 239000003345 natural gas Substances 0.000 claims abstract description 99
- 238000001816 cooling Methods 0.000 claims abstract description 97
- 150000001875 compounds Chemical class 0.000 claims abstract description 95
- 239000002826 coolant Substances 0.000 claims abstract description 57
- 239000007789 gas Substances 0.000 claims abstract description 46
- 230000006835 compression Effects 0.000 claims abstract description 28
- 238000007906 compression Methods 0.000 claims abstract description 28
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 18
- 230000008016 vaporization Effects 0.000 claims abstract description 16
- 239000000126 substance Substances 0.000 claims abstract description 13
- 239000002955 immunomodulating agent Substances 0.000 claims abstract description 12
- 229940121354 immunomodulator Drugs 0.000 claims abstract description 12
- 230000002584 immunomodulator Effects 0.000 claims abstract description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 52
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 28
- 229910052757 nitrogen Inorganic materials 0.000 claims description 26
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 14
- 239000001294 propane Substances 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 9
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- 230000008859 change Effects 0.000 claims description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 5
- 239000005977 Ethylene Substances 0.000 claims description 5
- 239000001273 butane Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 2
- LWSYSCQGRROTHV-UHFFFAOYSA-N ethane;propane Chemical compound CC.CCC LWSYSCQGRROTHV-UHFFFAOYSA-N 0.000 claims 1
- 238000005516 engineering process Methods 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 7
- 229930195733 hydrocarbon Natural products 0.000 description 7
- 150000002430 hydrocarbons Chemical class 0.000 description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 230000004087 circulation Effects 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 238000004781 supercooling Methods 0.000 description 3
- 230000007547 defect Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000005381 potential energy Methods 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- -1 alternatively Chemical compound 0.000 description 1
- 230000037237 body shape Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000012938 design process Methods 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- AEDZKIACDBYJLQ-UHFFFAOYSA-N ethane-1,2-diol;hydrate Chemical compound O.OCCO AEDZKIACDBYJLQ-UHFFFAOYSA-N 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000659 freezing mixture Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000012546 transfer 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
- F25J1/0002—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
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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
- F25J1/003—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
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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
- 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
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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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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- 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
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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
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- 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.
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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.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical 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
- F25J1/0211—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
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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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0277—Offshore use, e.g. during shipping
- F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
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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
- 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
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
-
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Ocean & Marine Engineering (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A kind of equipment (100) for making natural gas liquefaction includes :-compressor (105), for the first Vaporizing cooling agent chemical mixture, device (110), for being fractionated the mixture of compression for heavy distillat and light fraction,-the first heat exchange body (115), for carrying out heat exchange between the heavy distillat and natural gas of the first mixture, with at least cooled natural gas,-the second heat exchange body (120), for carrying out heat exchange between the natural gas of the cooling in the light fraction of the first mixture and the first heat exchange body, to make natural gas liquefaction, with-return pipe (125), for making the first Vaporizing cooling agent composition in heat exchange body be back to compressor (105), third heat exchange body (130, 135), positioned at the first heat exchange body (115) The downstream of the outlet (121) of the liquefied natural gas of the upstream or the second heat exchange body (120) of middle gas inlet (116), for carrying out heat exchange between natural gas and the second cooling immunomodulator compounds, with-device (140,145), for compressing the second vapourised compound.
Description
Technical field
The present invention relates to a kind of equipment of liquefied natural gas, the method for liquefied natural gas and the ship including the equipment.This hair
The bright marine or land liquefaction for being particularly suitable for natural gas.
Background technique
Compared to not liquefied natural gas is transported, liquefied gas allows with lesser volume transportation natural gas.
In past many decades, due to scale economy, liquefaction technology is absorbed in large-scale gas production capacity.
It needs very big investment in this way, implementing the technology and there is very high transportation cost (to liquefy and connect in ocean
Receive facility).As a result, the trend of liquefying power first is to improve the natural gas volume of conveying, to obtain scale economy and make this
A little projects are economically more attractive.Secondly, the investment carried out to implement these technologies concentrates in this scale, and liquid
The building of change method must be it is most effective, to reduce subsequent operation cost to the maximum extent.
Nowadays, the quantity of large-scale project is greatly reduced, and people are to the liquefaction using natural gas or biogas production low capacity
Natural gas restarts to generate interest.
In fact, the upgrading of mini gas, bi-product gas and biogas is new opportunity, people and government are increasingly
The environmental consciousness of enhancing will contact no natural gas transportation and/or dispense the hope of the independent consumer in the area of infrastructure
This new opportunities are especially supported in prestige.It is mentioned however, these opportunities are too small so that it cannot being suitable for large-scale production for these technologies
For sensible argument (conversion of traditional technology be it is inappropriate, since they are excessively complicated and cannot be used to support these technologies
Economic feasibility), therefore, it is necessary to propose new technology to cope with two significant challenges relevant to liquefying on a small scale:
In order to be minimized production cost, reduction investment cost as much as possible keeps efficiency as high as possible simultaneously；With
The efficiency of improvement method is to minimize the loss of product: the gas volume of upgrading is small, this makes each point
Son is all critically important.
Nowadays, it is developed rapidly to the natural gas resource of sea and offshore, causes to solve using the technology suitable for marine environment
Scheme, referred to as " FLNG " (represent " floating liquefied natural gas " (" Floating Liquefied Natural Gas ")).
Particularly, it is known that the liquefaction cycle of several types:
Cascade cycle；
Freezing mixture circulation；With
Extended Cyclic (expansion cycles).
Combination of the liquefaction cycle based on these circulations or these circulations.This is clearly " whole convolution cascade-type liquefaction
The example of (Integral Incorporated Cascade) " process, i.e. CII (" cascade int é grale incorpor é
The abbreviation of e ").
In CII system:
Coolant mixture is compressed, heavy distillat and light fraction are then fractionated into；
Heavy distillat is used in the first plate heat exchanger, is carried out heat exchange in heavy distillat and natural gas, is allowed to cool；
Compress light fraction；
Light fraction is for carrying out heat exchange for heavy distillat and cooling natural gas, so that naturally in the second plate heat exchanger
Gas is liquefied；With
Then the two kinds of fractions reheated in mixture are collected, and supply compression again.
There are several defects for this system:
Plate heat exchanger is very sensitive to the distribution of fluid, this proposes ocean applicability problem to ocean application；
Coolant mixture contains a large amount of components, especially heavy compounds, and these compounds are in specific pressure
It is crystallized in the heat exchanger under the conditions of temperature, and it is difficult to predict；With
This method has limited flexibility (especially in terms of operating flow velocity), and the production of each compression set
Ability is limited.
In CII method, coolant mixture is nitrogen and hydrocarbon (methane, ethane, iso-butane, normal butane, isopentane and positive penta
Alkane) mixture.The part evaporation of the mixture can make natural gas cooling and liquefaction under low pressure, and make the LNG generated
Supercooling:
The evaporation of heavy distillat (gas at the top of fractionating column) under low pressure can be provided to natural gas in coolant mixture
Carry out cooling necessary negative heat；With
Light fraction can make natural gas liquefaction and make LNG supercooling.
When being exported from switched line, coolant mixture evaporating completely.
For CII system, major defect is:
- CII method is produced for land extensive LNG and is developed；
The flexibility of this method is not fine: any deviation operation/design point, efficiency can be all remarkably decreased；
Coolant mixture includes too multiple components (hydrocarbon), keeps logistics and operating condition more complicated；
Storage increases the weight of facility, this is most important to Offshore Units；
This method has difficulties in terms of supplying ethane, this causes very big difficulty to Offshore Units；
It, should since there are the risks of crystallization for the pentane (different C5 (iC5) and positive C5 (nC5)) that contains in coolant mixture
There is the risk for changing equipment (converter) in method；
The efficiency of this method is limited to the size and working condition of converter；With
This method there is a problem of installing with offshore set-up it is related (if distribution is incorrect, the performance of plate heat exchanger
It is remarkably decreased).
CII method depends on the single compressed line using centrifugal compressor.
Centrifugal compressor is used for compressed gas, the result is that improving its pressure.Centrifugal compressor is furnished with around by turbine
Machine or the wheel of the axis of motor drive rotation.These rotating wheels make the kinetic energy for including in gas be converted into potential energy, to increase
Its pressure.
Since the possible pressure increase that wheel can be realized is limited, it is therefore necessary to increase their quantity so as to reality
Existing desired discharge pressure.
These wheels are included in the main body for being known as " casing ".One casing may include eight to most ten wheels；
Quantity is bigger, and compressor is more likely to occur stability problem.
Compression is the core of liquifying method.In fact, each of obtaining additional efficient point on the compressor, will increase
The liquefied natural gas of production.
In addition, compressor set is capital intensive (capital-intensive) type component in liquefaction unit.
The efficiency for improving centrifugal compressor causes investment to increase.On the contrary, reducing investment leads to the reduction of solution efficiency
And/or flexibility significantly reduces.
The economic value of compressor is directly related to the quantity of casing.In fact, casing quantity is more, investment is higher, but
Operating flexibility is bigger.On the contrary, casing quantity reduces, causes operating flexibility to reduce, be sometimes associated with loss of efficiency.
Therefore, challenge of the invention is to provide better scheme between efficiency and investment, so as to as wide as possible
Satisfactory performance level is kept in opereating specification.
The compressor set of CII method includes low-voltage and medium voltage part and high pressure compressed part.Compression step is combined in one
In a, two or three casings.
It low-voltage and medium voltage part can be mixed with low pressure compression coolant when coolant mixture is exported from low temperature switched line
Close object.
High-pressure section can compress the light fraction of coolant mixture, this can be mentioned for liquefaction and the supercooling of liquefied natural gas
For required negative heat.
Low pressure and high-pressure section in compressor set are driven by same axis, causes to have between the turbine of these parts
Single rotation speed.The rotation speed can come area by using relative to the multiplication mechanism between uniaxial rotation speed
Point.However, in the case where being with or without multiplication mechanism, rotation speed must be it is proportional or identical, be based on the feelings
Condition, this makes compressor set not flexible when the flow velocity for entering each part is different or proportional.This may cause mechanically stable
Property problem.
In addition, observing that efficiency declines to a great extent in high-pressure section, when it is desirable that including in a casing by two parts even
It is more significant.
Finally, this configuration is not very flexibly which has limited the area of opportunity being able to solve: if deviateing equipment size
Operating point (natural gas and accurate working condition), it can be observed that efficiency declines, this may be significantly, also it is possible to deposit
In mechanical stability problems, this leads to more frequent maintenance.
Current CII system has the disadvantage in that
Change in flow between the low-pressure section and high-pressure section of compressor set leads to imbalance between the two parts,
This may cause the mechanical instability problem during being turned off and on the stage；
Observe that efficiency is remarkably decreased between low-pressure section and high-pressure section；With
Limited flexibility of the compressor set in terms of flow rates and composition.
System is known, such as system described in document WO2011/039279.In such a system, hydrocarbon stream exists
It is separated in first fractionation apparatus, to generate the first hydrocarbon stream of the first hydrocarbon stream of top and lower part.The stream at top is liquefied, and then at least one
Part is cooled down by coolant fluid, to provide the coolant flow of cooling liquefaction hydrocarbon stream and heat.Then the liquefaction hydrocarbon stream of the cooling
It is inflated and stores.
Therefore, this document describe a kind of liquifying method, which uses recycles in separated cooling circuit
Three kinds of different pure cooling immunomodulator compounds.The description is difficult to carry out, especially from the perspective of operation, supply/logistics, and
Need big area for implementing.
Document " new trend (the New trends in LNG process of LNG technological design of E.Flesh et al.
Design the description in) " is also known.This description has several limitations:
In order to obtain the efficiency for the low temperature switched line being architectural limitation, technology needs are observed between lower part and top
To surface area ratio, which has limited the operating flexibilities of the technology；
There are heavy compounds in coolant mixture (pentane), if deviateed in the method design process specified
Opereating specification, then heavy compounds can crystallize and cause equipment damage.
Summary of the invention
It is an object of the invention to overcome all or part of drawbacks described above.
For this purpose, according in a first aspect, the present invention relates to a kind of for making the equipment of natural gas liquefaction, comprising:
It is used for the compressor of the first Vaporizing cooling agent chemical mixture,
For the mixture of compression to be fractionated the device for heavy distillat and light fraction,
The heat between heavy distillat and natural gas for exchanging the first mixture is main with the first of at least cooled natural gas
Body,
For exchange the first mixture light fraction and first exchange main body in cool down natural gas between heat with
Make the second main body of natural gas liquefaction, and
The first coolant mixture vaporized in heat exchange body is set to be back to the pipeline of compressor,
Comprising:
The outlet of the liquefied natural gas of the upstream of gas inlet in the first exchange main body or the second exchange main body
Downstream, for exchanging the third main body of the heat between natural gas and the second cooling immunomodulator compounds, and
Compress the device of the second vapourised compound.
When the upstream of the entrance of the natural gas in the first exchange main body is arranged in third exchange main body, the equipment can be with
The precooling of natural gas is executed before executing cooling by the first exchange main body.
When the downstream of the liquefied natural gas outlet of the second exchange main body is arranged in third exchange main body, the appearance of the equipment
Amount increases.
This configuration increases the advantages of traditional CII is configured by reducing its disadvantage, especially by following manner:
Reduce the flow velocity of coolant mixture and the influence to equipment energy consumption；
It reduces the weight of device: reducing the size of the compressor for coolant mixture, simplifies logistics and reduce scene
Storage capacity；
Reduce the scale of the equipment；With
Production and efficiency is maximized by minimizing number of devices.
Therefore, the present invention uses single initial cooling mixture, the single initial cooling mixture due to primary or
It is fractionated twice and is broken down into two or three of the mixture recycled in single closed circuit.The number of devices used greatly subtracts
It is few, and simplify control.
In some embodiments, the upstream of the gas inlet of the first exchange main body, institute is arranged in third exchange main body
Stating equipment includes:
It is used to cool down the device of the second compression compound, and
For the second cooling compound to be transferred to the pipeline of third exchange main body.
These embodiments can produce the precooling circuit of natural gas.
In some embodiments, second compound is pure material, including nitrogen, propane and/or ammonia, alternatively, nitrogen
With the mixture of propane.
Second compound is formed using this composition, can be entered in the natural gas by the first and second exchange main body shapes
At switched line before cooled natural gas.This precooling can simplify/limit ingredient in the used first cooling mixture
Quantity, this also can reduce the size of the exchange surface between natural gas and the first cooling mixture.
In some embodiments, the first cooling mixture includes nitrogen and methane and following at least one compound:
Ethylene；
Ethane；
Propane；And/or
Butane.
The energy supply minimum in liquefied natural gas system can be used using this mixture.
In fact, heavy compounds are used in the first coolant mixture in the CII system implemented at present, these
Compound has the advantages that ensure that the first mixture vaporizes before entering the first compressor.
However, according to the content of these heavy compounds and the specific operation condition that may be temporarily exceeded, these heavys
Compound has the shortcomings that crystallize in the most cold part of exchanger.So far, there are no specific general limitations can be true
Fixed when to crystallize, this leads to uncertain and damage risk.However, despite the presence of this disadvantage, but favor at present in
Such compound is still used using those skilled in the art that gaseous state inputs the first compressor.
In some embodiments, the upstream of the gas inlet of the first exchange main body, institute is arranged in third exchange main body
Stating equipment includes, in the downstream of the liquefied natural gas outlet of the second exchange main body:
For exchanging the 4th exchange main body of the heat between liquefied natural gas and nitrogen；
For compressing the device of vaporization nitrogen；
For cooling down the device of compressed nitrogen；With
The route for being transported to the 4th exchange main body for nitrogen will to be cooled down.
These embodiments can obtain the combination of the natural gas and then cooling liquefied natural gas of precooling.
In some embodiments, as the equipment of present subject matter second of the device for cooling down second compound
It include circuit between the outlet of compound and third exchange main body, which passes through main intracorporal first mixture of the first exchange
Heavy distillat cools down second compound.
These embodiments can cool down the second compound in the cascade exchanger formed by the first and second exchangers.
In some embodiments, a part of cooling circuit is configured to by exchanging the first mixing in main body with second
The light fraction of object exchanges heat to cool down second compound.
These embodiments allow to the second change in the cooling cascade exchanger formed by the first and second exchangers
Close object.
In some embodiments, the first exchange main body and/or the second exchange main body are coil exchangers.
In some embodiments, the device of cooling second compound is the heat exchanger between second compound and water.
According to second aspect, the present invention relates to ship, the ship includes making setting for natural gas liquefaction as present subject matter
It is standby.
According to the third aspect, the present invention relates to the methods for making natural gas liquefaction, comprising:
The step of compressing the first Vaporizing cooling agent chemical mixture,
The step of compressed mixture is fractionated into heavy distillat and light fraction,
It carries out walking with the first heat exchange of at least cooled natural gas between the heavy distillat and natural gas of the first mixture
Suddenly,
It carries out between natural gas cooling in the light fraction and the first exchange step of the first mixture so that natural gas liquid
The second heat exchange steps changed, and
The step of making the first coolant mixture vaporized in heat exchange body return to compression step,
Comprising:
Input the first exchange step natural gas before or from the second exchange step output liquefied natural gas it
Afterwards, the third heat exchange steps carried out between natural gas and the second cooling immunomodulator compounds, and
The step of compressing the second vapourised compound.
Due to the specific purpose of ship and method as present subject matter, advantages and features and as the dress of present subject matter
It is similar for setting, therefore is not repeated herein.
Detailed description of the invention
Other advantages of the invention, purpose and special characteristic will be from below to the devices, ship and side as present subject matter
The non restrictive description of at least one particular implementation of method becomes apparent, with reference to attached drawing, in which:
- Fig. 1 schematically shows the first particular implementation of the equipment as present subject matter；
- Fig. 2 schematically shows a kind of particular implementation of the ship as present subject matter；
- Fig. 3 indicates that the first particular series as the method for present subject matter walk schematically and in the form of logic chart
Suddenly；
- Fig. 4 schematically shows second of particular implementation of the equipment as present subject matter；
- Fig. 5 indicates that the second particular series as the method for present subject matter walk schematically and in the form of logic chart
Suddenly；
- Fig. 6 schematically shows the third particular implementation of the equipment as present subject matter；
- Fig. 7 schematically shows a kind of particular implementation of the compressor of the equipment as present subject matter；With
- Fig. 8 indicates that the third particular series as the method for present subject matter walk schematically and in the form of logic chart
Suddenly.
Specific embodiment
This specification provides in a non-limiting manner, a kind of each feature of embodiment can in an advantageous manner with appoint
Any other feature combination of what other embodiments.
Please note that attached drawing is not in proportion.
Fig. 1, it is not in proportion, show the schematic diagram of the embodiment as present subject matter equipment 100.The equipment
100 are used for liquefied natural gas, comprising:
Compressor 105 is used for the first Vaporizing cooling agent chemical mixture,
Device 110, for being fractionated the mixture of compression for heavy distillat and light fraction,
- the first main body 115, the heat between heavy distillat and natural gas for exchanging the first mixture, at least cooling
Natural gas,
- the second main body 120, for exchanging the light fraction of the first mixture and exchanging the cooled natural gas of main body first
Between heat, with liquefied natural gas, and
Pipeline 125, for making vaporized the first coolant mixture in heat exchange body be back to compressor 105,
Comprising:
Third main body 130 or 135, the upstream of the gas inlet 116 in the first exchange main body 115 or the second friendship
The downstream of the outlet 121 of the liquefied natural gas of change owner body 120, for exchanging the heat between natural gas and the second cooling immunomodulator compounds
Amount, and
Device 140 or 145, for compressing the second vapourised compound.
Compressor 105 is, for example, centrifugal compressor, is rotated equipped with around by turbine or the axis of motor drive
Wheel.The wheel of this rotation to include that kinetic energy in gas is converted to potential energy, to increase the pressure of the gas.For
Increase carried out compression, the quantity of wheel is increased to realize defined discharge pressure.
The input pressure of compressor 105 is, for example, at least about 2 bars of absolute value.The compression factor generated in compressor 105 is such as
Between 2 and 6.
This compressor 105 is for example configured to the first coolant mixture of compression, which includes nitrogen
Gas, methane and following at least one compound:
Ethylene；
Ethane；
Propane；And/or
Butane.
The composition of first compound is adjusted according to the ingredient of natural gas to be liquefied in equipment.This adjustment is root
According to the gas componant of the switched line formed by the first permutoid 112 and the second permutoid 120 steam characteristics curve (i.e. pressure/
Equalized temperature) come what is implemented.
Purpose using propane is the volatility between the heavy compounds and light compounds balanced in the first mixture
Difference.
This compressor 105 includes for the import (unnumbered) of vaporized coolant mixture and for the cold of compression
But the outlet (unnumbered) of agent composition.
The coolant mixture of compression is cooling preferably in the 5th heat exchanger 106.Heat exchanger 106 is, for example, that cold source is
The tubular exchanger of air or water.The temperature of cold source is lower, and this method is more effective.Preferably, highest cooling temperature is equal to sky
The temperature of gas or water adds 15 degrees Celsius.
Coolant mixture, it is cooling preferably in the 5th heat exchanger 106, it is provided to fractionating device 110.Fractionating device
110 be, for example, fractionating column.
The fluid for inputting fractionating column is two-phase, a part be it is gaseous, a part is liquid.Gaseous fraction is in tower
Middle flowing is simultaneously flowed out from tower top, and the fraction of liquid is flowed out from bottom.
Fractionating device 110 includes:
The entrance (unnumbered) of compressed coolant mixture；
The outlet (unnumbered) of the light fraction of coolant mixture, positioned at the bottom of fractionating device 110；Know
The outlet (unnumbered) of the heavy distillat of coolant mixture, the outlet relative to light fraction are located at fractionating device 110
Top.
Preferably, the light fraction left from fractionating device 110 enters the first exchange main body 115, and is passed through the first heat
The heavy distillat for exchanging main body 115 is cooling.According to operating condition, light fraction can also be used as natural gas from the first exchange main body 115
The cold source of heat exchange that occurs when entering of entrance 116.
In some preferred modifications, fractionating device 110 further includes the entrance for a part of light fraction that flows back, and should
Part light fraction is for example collected in return tank 111.
Therefore, fractionating device 110 includes preferably filler, can improve air-flow and the liquid distillate from return tank 111
Between mass transfer, absorb most heavy compound in gaseous fraction, can be obtained on head and be rich in the gas of nitrogen and methane
Stream.
Fractionating device 110 is preferably provided with engagement (meshing), to limit the drop carried in gaseous fraction.
Return tank 111 is connected with the fraction outlets of fractionating device 110, carries out in the first main body 115 or without in
Between exchange, and light fraction is separated from heavy distillat residue with similar operation, wherein heavy distillat residue is by light fraction
Unexpectedly exported from fractionating device 110.
Return tank 111 is preferably provided with engagement, to limit the drop carried in gaseous fraction.
Preferably, it is compressed using the second compressor 112 and leaves fractionating device 110 or return tank 111 (when the return tank
In the presence of 111) light fraction.
Second compressor 112 is, for example, centrifugal compressor.This centrifugal compressor is preferably by the position of compressor 105
Place is set using turbine drives, when compressor 105 is centrifugal compressor.
For example, about 40 bars of pressure absolute value of second compressor 112 output, compression ratio is preferably between 2 and 4.
Regardless of carrying out in the second compressor 112 or without compression, light fraction is preferably cold in the 6th heat exchanger 113
But.
Heat exchanger 113 is, for example, the pipe heat exchanger that cold source is air or water.The temperature of cold source is lower, and cooling efficiency is got over
It is high.Preferably, highest cooling temperature is equal to air or the temperature of water adds 15 degrees Celsius.The fluid of generation supplies cooled natural gas
Required cold or negative heat.
Regardless of whether being compressed in the second compressor 112, also regardless of whether being carried out in the 6th exchanger 113 cold
But, light fraction is transported in first heat exchanger 115.
First heat exchanger 115 is, for example, coil exchanger, and light fraction is used as cold source wherein, and natural gas is as heat source.
Preferably, first heat exchanger 115 and second heat exchanger 120 are made of single coil exchanger.
Natural gas enters first heat exchanger 115 by entrance 116.
The light fraction that the natural gas in main body 115 vaporize in heat exchanging process is exchanged with first is preferably entered rotary drum
(drum) 114, rotary drum 114 is configured to light fraction being divided into two parts, and a portion is than another part weight.
Preferably, equipment 100 includes the valve 136 of 114 upstream of rotary drum.For example, the valve makes the gaseous state of the first mixture
About 20 to 25 bars of demi-inflation.
Two parts of light fraction are transported to the second exchange main body 120, and light fraction is preparatory in the first heat exchange body 115
Cooling natural gas carries out being used as cold source in heat exchanging process.
When equipment 100 is using rotary drum 114, after the heavies of light fraction pass through the second exchange main body 120, in expander
It expands in 118, is then transported in compressor 105 by return pipe 125.
Expander 118 substitutes valve 123 or in parallel with valve 123.
In some variations, between expander 118 and compressor 105, the heavies of light fraction are compressed, and are infused again
Enter into the second exchange main body 120.
Light fraction in light fraction is delivered to compressor 105 by return pipe 125.
In some variations, the light fraction of light fraction expands in valve 122 when leaving the second permutoid 120, and
Before being directed to compressor 105, it is reinjected into second permutoid 120.
For example, valve 122 generates the pressure that expansion reaches about 4 to 5 bars according to the pressure drop of downstream loop.
The heavies for leaving the coolant mixture of fractionating device 110 are transported in the first exchange main body 115, and
With in the exchange process of natural gas be used as cold source.
In some variations, equipment 100 includes the expander 127 in parallel with valve 122.
Preferably, equipment 100 includes expander 127, and does not include valve 122.
In some variations, after expanding in adjuster 119, before being sent to compressor 105, double distilled separates the
One exchange main body 115 is simultaneously reinjected into the first exchange main body 115.
For example, according to the pressure drop of the first exchange main body 115, adjuster 119 generates the pressure that expansion reaches about 4 to 5 bars.
In some variations, return pipe 125 includes the rotary drum between the first exchange main body 115 and compressor 105
126。
The rotary drum 126 may insure that when being input to the first compressor 105, first coolant mixture is only gaseous state.
Preferably, rotary drum 126 carries drop equipped with engagement to limit gaseous fraction.
Preferably, equipment 100 includes the pipeline that a part of rotary drum 126 is connected to fractionating device 110, for receiving the
The liquid portion of one mixture.Preferably, the pipeline is equipped with pump.Preferably, which collects according to a part of rotary drum 126
Liquid level driven by sensor, to receive the liquid portion of the first mixture.
In this way, it will be understood that due to two continuous cooling steps, natural gas is liquefied.First step is in the first exchange
It is carried out in main body 115, second step carries out in the second exchange main body 120.
Natural gas recycles in the first main body 115 and the second main body 120, preferably with the first coolant mixture adverse current
Mode recycles.
Cooled natural gas preferably leaves the first main body 115 with -30 DEG C of temperature.Then, cooled natural gas is excellent
Choosing is delivered to fractionating section (not shown) to isolate any condensate from gaseous fraction.Gaseous fraction is delivered to the second main body
120 to be liquefied.
Other than above-mentioned two step, the present invention increases third cooling step before or after first two steps are suddenly.
In the first scenario, third exchange main body 130 is located at the gas inlet 116 in the first exchange main body 115
Upstream.It is, for example, tubular exchanger that third, which exchanges main body 130, uses the second cooling immunomodulator compounds as cold source, and as heat
The natural gas in source enters equipment 100 and is just liquefied.
Second compound is, for example, the pure material being made of the mixture of nitrogen, propane and/or ammonia or nitrogen and propane.
Preferably, when using ammonia, ammonia is used alone.
In the latter case, the cooling main body 135 of third is located at the liquefied natural gas outlet 121 of the second exchange main body 120
Downstream.It is, for example, tubular exchanger that third, which exchanges main body 135, uses the second cooling immunomodulator compounds as cold source, as heat
Source, the liquefied natural gas being discharged from equipment 100 are stored or use.Liquefied natural gas can be in storage in this way
It is preceding that atmospheric pressure is expanded to by adjuster (not shown).The boil-off gas collected in the storage of liquefied natural gas is known as " BOG "
(representing " boil-off gas ") can re-inject equipment 100 in the position that gaseous fraction leaves distillation stage, and distillation stage is located at first
It exchanges between main body 115 and the second exchange main body 120.
Here the cooling compound of second is, for example, liquid nitrogen.
In the downstream of third main body 130 or 135, equipment 100 includes device 140 or 145, for compressing second compound.
Compressor 140 or 145 is, for example, centrifugal compressor.
In some preferred embodiments, equipment 100 has both the cooling step of upstream and the cooling step in downstream.
In these embodiments, third exchange main body 130 is designated as being located at the exchange of the first exchange 115 upstream of main body
Main body, and the 4th exchange main body 135 is designated as the exchange main body positioned at 120 downstream of the second permutoid.Second coolant
It closes object and is designated as the coolant mixture used in third main body 130, also, third coolant mixture is designated as
Coolant mixture used in 4th exchange main body.
In some embodiments, equipment 100 includes:
Device 150, for cooling second compound compressed in compression set 140；With
Pipeline 155, for compressed second compound to be delivered to third exchange main body 130.
Cooling device 150 is, for example, the vaporized during exchange the natural gas progress heat exchange in main body 130 with third
Heat exchanger between two compounds and air or water.
In some embodiments, as shown in Figure 1, outlet 131 and third permutoid in the second compound of device 150
Between 130, equipment 100 includes circuit 170, for cooling down the with the heavy distillat of the first mixture in the first exchange main body 115
Two compounds.
Can be by the way that second cooling the first exchange main body 115 of compound input be realized cooling circuit 170, second is cooling
Compound passes through the first exchange main body 115 as relative to the heat source of heavy distillat and any light fraction.Second vapourised compound can
Simultaneously as the cold source relative to the natural gas for being input to the first main body 115 by gas inlet 116.
In some variations, the second vapourised compound leaves the first main body 115, expands in adjuster 124, then again
Inject the first main body 115 or the second main body 120.
According to the pressure drop of upstream line, second compound can be expanded to 3 to 4 bars of pressure.
The purpose of cooling circuit 170 is the cooling for promoting to occur in cooling device 150.
In some embodiments, as shown in Figure 1, a part of cooling circuit 170 is configured as by exchanging with second
The light fraction of the first mixture in main body 120 carries out heat exchange to cool down second compound.
In these embodiments, by the cooling second compound of the first exchange 115 heat exchange of main body by injection the
Two exchange main bodys 120.Then, the second vapourised compound passes through as the heat source relative to the first coolant mixture light fraction
Second exchange main body 120.Meanwhile second vapourised compound can be used as relative to input second exchange main body 120 natural gas
Cold source.
In some embodiments, equipment 100 includes:
Device 160, for cooling down compressed nitrogen；With
Route 165, for the nitrogen cooled down to be transported to the 4th exchange main body 135.
Cooling device 160 is, for example, the exchanger between the third mixture and air or water compressed.
Natural gas can be pre-processed before third exchanges main body 130.
Compressor used in the embodiment and compression set 105,112 and 140 can be by the compressors shown in Fig. 6
605, it 610 and 620 replaces, their function is similar.
Fig. 2, it is not in proportion, show the schematic diagram of the embodiment of the ship 200 as present subject matter.The ship
200 include:
Equipment 100, for liquefied natural gas as shown in Figure 1；
Equipment 400, for liquefied natural gas as shown in Figure 4；
Equipment 600 is used for liquefied natural gas as shown in FIG. 6.
Fig. 3 shows the particular series step as the method 300 of present subject matter in the form of schematic diagram and logic chart.
The method 300 of the liquefied natural gas includes:
Step 305, the first Vaporizing cooling agent chemical mixture is compressed,
Step 310, compressed mixture is fractionated into heavy distillat and light fraction,
- the first heat exchange steps 315, the heat exchange carried out between the heavy distillat and natural gas of the first mixture is at least
Cooled natural gas,
- the second heat exchange steps 320, in the light fraction and the first exchange step of the first mixture cooling natural gas it
Between carry out heat exchange with liquefied natural gas, and
Step 325, the first coolant mixture vaporized in heat exchange body is made to return to compressor step,
Comprising:
Before the natural gas for inputting the first heat exchange steps or liquefied natural gas is being exported from the second heat exchange steps
Later, the third heat exchange steps 330 carried out between natural gas and the second cooling immunomodulator compounds, and
Step 335, the second vapourised compound is compressed.
This method 300 using equipment 100 as shown in Figure 1 for example by being implemented.It is appreciated that equipment 100 is all
Modification, all embodiments and all embodiments can be exchanged according to the step of method 300.
Fig. 4, it is not in proportion, show a kind of schematic diagram of embodiment of the equipment 400 as present subject matter.
Equipment 400 for liquefied natural gas includes:
Compressor 105 is used for the first Vaporizing cooling agent chemical mixture,
Device 110, for compressed mixture to be fractionated into heavy distillat and light fraction,
- the first main body 115, for carrying out heat exchange between the heavy distillat and natural gas of the first mixture, so as at least
Cooled natural gas,
- the second main body 120, between natural gas cooling in the light fraction of the first mixture and the first exchange main body
Heat exchange is carried out, with liquefied natural gas, and
Pipeline 125, for making the first coolant mixture vaporized in heat exchange body return to compressor,
Include:
Adjuster 405 is used for liquefied natural gas,
Collector 410, the boil-off gas for being generated during the gas expansion in adjuster 405, and
Pipeline 415, for the boil-off gas of entrance to be injected into the second permutoid.
In Fig. 4, and the relevant various devices of the first coolant mixture are identical as Fig. 1 or device shown in Fig. 6, packet
Include the particular variant shown and embodiment with reference to Fig. 1 and Fig. 6.These devices are:
Compressor 105,
Exchanger 106,
Fractionating device 110,
Return tank 111,
Compressor 112,
Exchanger 113,
Rotary drum 114,
- the first exchange main body 115,
Gas inlet 116,
Expander 118,
Adjuster 119,
- the second exchange main body 120,
The outlet 121 of the liquefied natural gas of-the second exchange main body 120,
Adjuster 122,
Expander 126,
Return pipe 125,
Rotary drum 126, and
Valve 136.
In this way it is possible to understand, due to two continuous cooling steps, natural gas is liquefied.First step is
It is carried out in one exchange main body 115, second step carries out in the second exchange main body 120.
Between the two steps, i.e., in the outlet (unnumbered) of the cooled natural gas of the first main body 115 and for cooling down
Natural gas enters between the entrance (unnumbered) of the second main body 120, and equipment 400 preferably includes fractionating section, the fractionating section quilt
It is configured to remove condensate from air-flow.
By outlet 121 leave the second main body 120 liquefied natural gas pass through adjuster 405, adjuster 405 be configured to by
Liquefied natural gas is expanded to atmospheric pressure.
Adjuster 405 is, for example, the valve using Joule-Thomson effect (Joule-Thomson effect).
It is this to expand the appearance for leading to boil-off gas, i.e. BOG.
The BOG generated in this way is collected in collector 410, and is injected into the second exchange master via pipeline 415
Body 120.Upstream in fractionating section (if there is such part), internal or downstream can occur for the injection.
Collector is, for example, gas/liquid separation rotary drum 410, carries drop equipped with engagement to limit gaseous fraction.
Preferably, pipeline 415 compresses the gaseous fraction for leaving collector 410 equipped with compressor 416, compressor 416.
In some embodiments, such as shown in Fig. 4, third exchanges main body 420 and is located in the first exchange main body 115
The upstream of gas inlet 116.The third exchange main body 420 is, for example, tubular exchanger, uses the second coolant chemical combination
As cold source, the natural gas as heat source enters equipment 400 and is just liquefied object.
Therefore, equipment 400 includes the compressor 425 in second vapourised compound in third exchange 420 downstream of main body.It is described
Compressor 425 is, for example, centrifugal compressor.
Second compound, the pure object being e.g. made of the mixture of nitrogen, propane and/or ammonia or nitrogen and propane
Matter.
In some embodiments, equipment 400 includes:
Device 430, for cooling down the second compression compound；With
Pipeline 435, for the second cooling compound to be transferred to third exchange main body 420.
Cooling device 430 is, for example, the exchanger between the second compression compound and water or ethylene glycol water.
In some embodiments, as shown in figure 4, the device 430 for cooling down second compound second compound
Between outlet 421 and third permutoid 420, equipment 400 includes circuit 440, for mixed with first in the first exchange main body 115
Close the cooling second compound of heavy distillat of object.
Can be by the way that second cooling the first exchange main body 115 of compound input be realized cooling circuit 440, second is cooling
Compound passes through the first exchange main body 115 as relative to the heat source of heavy distillat and any light fraction.Meanwhile second cools down chemical combination
Object can be used as the cold source relative to the natural gas for being input to the first main body 115 by gas inlet 116.
In some variations, the second vapourised compound leaves the first main body 115, expands in adjuster 424, then infuses again
Enter the first main body 115 or the second main body 120.
For example, second compound is expanded to 3 to 4 bars of pressure when exporting from adjuster 424.
The purpose of the cooling circuit 440 is the cooling for promoting to occur in cooling device 430.
As shown in Figure 1, the circuit 440 can also include second part in the second exchange main body 120.
In some particular implementations, the first cooling mixture includes nitrogen and methane and following at least oneization
Close object:
Ethylene；
Ethane；
Propane；And/or
Butane.
Fig. 5 schematically shows the particular implementation of the method 500 as present subject matter.For liquefied natural gas
Method 500 include:
Step 505, the first Vaporizing cooling agent chemical mixture is compressed,
Step 510, compressed mixture is fractionated into heavy distillat and light fraction,
- the first heat exchange steps 515, the heat exchange carried out between the heavy distillat and natural gas of the first mixture is at least
Cooled natural gas,
- the second heat exchange steps 520, the cooling natural gas of the light fraction of the first mixture and the first heat exchange steps it
Between the heat exchange that carries out with liquefied natural gas, and
Step 525, the first coolant mixture vaporized in heat exchange body is made to return to compressor step,
Comprising:
Step 530, liquefied natural gas is expanded；
Step 535, the boil-off gas generated in expansion step is collected；With
Step 540, boil-off gas is injected into the entrance of the second exchange main body.
This method 500 using equipment 400 as shown in Figure 4 for example by being implemented.It is appreciated that equipment 400 is all
Modification, all embodiments and all embodiments can be exchanged according to the step in method 500.
Fig. 6 and 7 schematically shows the particular implementation of the equipment 600 as present subject matter.For the day that liquefies
So the equipment 600 of gas includes:
- the first centrifugal compressor 605 is used for the first Vaporizing cooling agent chemical mixture；
Device 110, for compressed mixture to be fractionated into heavy distillat and light fraction；
Second centrifugal compressor 610 of light fraction,
- the first main body 115, for carrying out heat exchange between the heavy distillat and natural gas of the first mixture, so as at least
Cooled natural gas,
- the second main body 120, for the compression light fraction of the first mixture and in the first exchange main body it is cooling natural
Heat exchange is carried out between gas, with liquefied natural gas, and
Pipeline 125, for making the first coolant mixture vaporized in heat exchanger return to the first compressor,
Include:
Third main body 420, positioned at the upstream of the gas inlet 116 of the first exchange main body, in natural gas and second
Heat exchange is carried out between cooling immunomodulator compounds；
Third centrifugal compressor 620, for compress the second vapourised compound, first and third centrifugal compressor by
Common single turbine 630 drives；
- the first compressor and the common shell 635 of third compressor；
Device 430, for cooling down the second compression compound；With
Pipeline 435, for the second cooling compound to be transferred to third exchange main body 420.
Term " shell (casing) " refers to the shell (housing) including at least one compressor.Each compressor packet
Include one or more wheels.
In described Fig. 6:
Exchanger 106,
Fractionating device 110,
Return tank 111,
Exchanger 113,
- the first exchange main body 115,
Gas inlet 116,
Adjuster 119,
- the second exchange main body 120,
The outlet 121 of the liquefied natural gas of-the second exchange main body 120,
Adjuster 122,
Expander 127,
Return pipe 125,
Rotary drum 126,
Valve 136,
Third exchanges main body 420,
Conveyance conduit 435,
- the four exchange main body 430,
The outlet 421 of-the second cooling immunomodulator compounds,
Cooling circuit 400,
Adjuster 424,
Adjuster 405,
Collector 410, and
The flow in pipes 415,
Particular variant and embodiment identical as the related device that Fig. 1 or Fig. 4 is described, being described including Fig. 1 and 4.
Third compressor 620 corresponds to third compressor 140 shown in fig. 1.However, the third compressor 620 is by driving
The turbine of the first compressor 605 is moved to drive.First compressor corresponds to the first compressor 105 shown in fig. 1.
4th compressor 615 is configured for improving the pressure of the light fraction of the first coolant mixture light fraction.
4th compressor and the second compressor 610 share single, and second compressor 610 corresponds to shown in fig. 1 the
Two compressors 112.
In some preferred embodiments, as shown in Figure 6 and Figure 7, the equipment 600 of present subject matter includes:
- the four centrifugal compressor 615 is located at the second compressor 610 and second and hands over for the light fraction of the first mixture
Between change owner body 120, second and the 4th centrifugal compressor driven by shared single 640；With
The shell 645 that-the second compressor and the 4th compressor share.
In some preferred embodiments, as shown in fig. 6, the equipment 600 of present subject matter includes:
Separator 650, for separating the gas fraction and liquid distillate of compression light phase, the compression separation of the 4th compressor 615
Gas fraction；
Adjuster 625, the liquid distillate for the light phase in the second exchange main body heating；
The turbine 640 of-the four compressor, is driven by expansion energy.
Separator 650 is for example similar to return tank 114 shown in fig. 1.Adjuster for example with expander 118 shown in fig. 1
It is similar.
In some preferred embodiments, as shown in fig. 6, second compound includes nitrogen, propane and/or ammonia.
In some preferred embodiments, as shown in fig. 6, the first cooling mixture include nitrogen and methane and at least with
A kind of lower compound:
Ethylene；
Ethane；
Propane；And/or
Butane.
In some preferred embodiments, as shown in fig. 6, equipment 600 includes:
The adjuster 405 of liquefied natural gas；
The collector 410 of the boil-off gas generated during gas expansion in adjuster；
Boil-off gas is injected into the pipeline 415 of the second exchange main body.
In some preferred embodiments, as shown in fig. 6, equipment 600 is exported in the second compound of cooling device 430
It include circuit 440 between 421 and third exchange main body 420, circuit 440 is used for using the first mixing in the first exchange main body 115
The heavy distillat of object cools down second compound.
In some preferred embodiments, as described in Figure 6, the first exchange main body 115 and/or the second exchange main body 120
It is coil exchanger.
In some preferred embodiments, as shown in fig. 6, being the second change for cooling down the device 430 of second compound
Close the heat exchanger between object and water.
Fig. 8 schematically shows the particular implementation of the method 700 as present subject matter.The method 700 is used
In liquefied natural gas, comprising:
- the first centrifugal compressed step 705, centrifugal compressed Vaporizing cooling agent chemical mixture,
Step 710, compressed mixture is fractionated into heavy distillat and light fraction,
- the second centrifugal compressed step 715, centrifugal compressed light fraction,
- the first heat exchange steps 720 carry out heat exchange between the heavy distillat and natural gas of the first mixture at least cold
But natural gas,
- the second heat exchange steps 725, the cooled natural gas in the light fraction of the first mixture and the first exchange main body
Between carry out heat exchange with liquefied natural gas, and
Step 730, the first coolant mixture for vaporizing heat exchange steps returns to the first centrifugal compressed step,
Include:
In the upstream for the step 735 that natural gas is inputted to the first exchange step, in natural gas and the second cooling immunomodulator compounds
Between the third heat exchange steps 740 that carry out；
The third centrifugal compressed step 745 of-the second vapourised compound, first and third centrifugal compressed step by common list
A turbine drives；
First and the third compression step carried out in common shell；
Step 750, the second compound compressed in cooling third exchange step；With
Step 755, the second cooling compound is transferred to third exchange step.
The method 700 using equipment 600 as described in figs. 6 and 7 for example by being realized.It is appreciated that equipment 600
All modifications, all embodiments and all embodiments can also be exchanged according to the step in method 700.
Claims (11)
1. a kind of equipment (100) for making natural gas liquefaction includes:
Compressor (105) is used for the first Vaporizing cooling agent chemical mixture,
Device (110), for being fractionated the mixture of compression for heavy distillat and light fraction,
- the first heat exchange body (115), for carrying out heat exchange between the heavy distillat and natural gas of the first mixture, so that
Few cooled natural gas,
- the second heat exchange body (120), the day for the cooling in the light fraction of the first mixture and the first heat exchange body
Heat exchange is carried out between right gas, to make natural gas liquefaction, and
Return pipe (125), for making the first Vaporizing cooling agent composition in heat exchange body be back to compressor (105),
It is characterised by comprising:
Third heat exchange body (130,135), be located at the first heat exchange body (115) in gas inlet (116) upstream or
The downstream of the outlet (121) of the liquefied natural gas of the second heat exchange body of person (120), in natural gas and the second coolant
It closes and carries out heat exchange between object, and
Device (140,145), for compressing the second vapourised compound.
2. equipment (100) according to claim 1, wherein the third heat exchange body (130) is arranged described first
The upstream of the gas inlet (116) of heat exchange body (115), the equipment (100) include:
For cooling down the device (150) of the second compression compound；With
Second cooling compound is transferred to the pipeline (155) of the third heat exchange body (130).
3. equipment (100) according to claim 2, wherein the second compound is pure material, including nitrogen, propane
And/or the mixture of ammonia or nitrogen and propane.
4. equipment (100) according to claim 1-3, wherein the first cooling mixture include nitrogen and
Methane and a kind of at least following compound:
Ethylene；
Ethane；
Propane；And/or
Butane.
5. equipment (100) according to claim 1-4, wherein third heat exchange body (130) setting exists
The upstream of the gas inlet (116) of first heat exchange body (115), in the liquid of second heat exchange body (120)
Change the downstream of the outlet (121) of natural gas, the equipment (100) includes:
- the four heat exchange body (135), for carrying out heat exchange between liquefied natural gas and nitrogen；
For compressing the device (145) of vaporization nitrogen；
For cooling down the device (160) of compressed nitrogen；
For the pipeline (165) that nitrogen is transported to the 4th heat exchange body will to be cooled down.
6. equipment (100) according to claim 5, wherein the device (150) for cooling down the second compound is institute
State the heat exchanger between second compound and water.
7. equipment (100) according to claim 1-6, in the device for cooling down the second compound
It (150) include circuit (170) between second compound outlet (131) and the third heat exchange body (130), for using
The cooling second compound of the heavy distillat of the first mixture in first heat exchange body (115).
8. equipment (100) according to claim 7, wherein a part of the cooling circuit (170) be configured to by with
The light fraction of the first mixture in second heat exchange body (120) carries out heat exchange to cool down the second compound.
9. equipment (100) according to claim 1-8, wherein first heat exchange body (115) and/or
Second heat exchange body (120) is coil exchanger.
10. a kind of ship (200), which is characterized in that described in any item for making setting for natural gas liquefaction including claim 1-9
Standby (100).
11. a kind of method (300) for making natural gas liquefaction, comprising:
Step (305) compresses the first Vaporizing cooling agent chemical mixture,
Step (310), is fractionated into heavy distillat and light fraction for compressed mixture,
- the first heat exchange steps (315) carry out heat exchange between the heavy distillat and natural gas of the first mixture at least cooling
Natural gas,
- the second heat exchange steps (320), in the light fraction and the first heat exchange steps of the first mixture cooling natural gas it
Between carry out heat exchange so that natural gas liquefaction, and
The first coolant mixture vaporized in heat exchange body is returned to compressor step by step (325),
It is characterised by comprising:
Input the first heat exchange steps natural gas before or from the second heat exchange steps output liquefied natural gas it
Afterwards, the third heat exchange steps (330) carried out between natural gas and the second cooling immunomodulator compounds, and
The step of compressing the second vapourised compound (335).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1663183A FR3061277B1 (en) | 2016-12-22 | 2016-12-22 | DEVICE AND METHOD FOR LIQUEFACTING A NATURAL GAS AND SHIP COMPRISING SUCH A DEVICE |
| FR1663183 | 2016-12-22 | ||
| PCT/FR2017/053610 WO2018115659A1 (en) | 2016-12-22 | 2017-12-15 | Device and method for liquefying a natural gas and ship comprising such a device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110537064A true CN110537064A (en) | 2019-12-03 |
Family
ID=58358664
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780085095.3A Withdrawn CN110537064A (en) | 2016-12-22 | 2017-12-15 | Device and method for liquefied natural gas and the ship including the equipment |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20190310014A1 (en) |
| EP (1) | EP3559572A1 (en) |
| CN (1) | CN110537064A (en) |
| BR (1) | BR112019012890A2 (en) |
| FR (1) | FR3061277B1 (en) |
| WO (1) | WO2018115659A1 (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1184528A (en) * | 1995-04-18 | 1998-06-10 | 国际壳牌研究有限公司 | Cooling a fluid stream |
| EP1092931A1 (en) * | 1999-10-12 | 2001-04-18 | Air Products And Chemicals, Inc. | Hybrid cycle for the production of liquefied natural gas |
| CN102636000A (en) * | 2012-03-13 | 2012-08-15 | 新地能源工程技术有限公司 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
| CN102893108A (en) * | 2009-09-30 | 2013-01-23 | 国际壳牌研究有限公司 | Method of fractionating a hydrocarbon stream and an apparatus therefor |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2909616C (en) * | 2013-04-22 | 2021-03-09 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for producing a liquefied hydrocarbon stream |
-
2016
- 2016-12-22 FR FR1663183A patent/FR3061277B1/en active Active
-
2017
- 2017-12-15 EP EP17825589.9A patent/EP3559572A1/en not_active Withdrawn
- 2017-12-15 CN CN201780085095.3A patent/CN110537064A/en not_active Withdrawn
- 2017-12-15 WO PCT/FR2017/053610 patent/WO2018115659A1/en unknown
- 2017-12-15 US US16/470,218 patent/US20190310014A1/en not_active Abandoned
- 2017-12-15 BR BR112019012890A patent/BR112019012890A2/en not_active Application Discontinuation
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1184528A (en) * | 1995-04-18 | 1998-06-10 | 国际壳牌研究有限公司 | Cooling a fluid stream |
| EP1092931A1 (en) * | 1999-10-12 | 2001-04-18 | Air Products And Chemicals, Inc. | Hybrid cycle for the production of liquefied natural gas |
| CN102893108A (en) * | 2009-09-30 | 2013-01-23 | 国际壳牌研究有限公司 | Method of fractionating a hydrocarbon stream and an apparatus therefor |
| CN102636000A (en) * | 2012-03-13 | 2012-08-15 | 新地能源工程技术有限公司 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2018115659A1 (en) | 2018-06-28 |
| US20190310014A1 (en) | 2019-10-10 |
| FR3061277B1 (en) | 2019-05-24 |
| EP3559572A1 (en) | 2019-10-30 |
| FR3061277A1 (en) | 2018-06-29 |
| BR112019012890A2 (en) | 2019-11-26 |
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