CN104204698B - Liquefied natural gas is formed - Google Patents
Liquefied natural gas is formed Download PDFInfo
- Publication number
- CN104204698B CN104204698B CN201380017937.3A CN201380017937A CN104204698B CN 104204698 B CN104204698 B CN 104204698B CN 201380017937 A CN201380017937 A CN 201380017937A CN 104204698 B CN104204698 B CN 104204698B
- Authority
- CN
- China
- Prior art keywords
- natural gas
- refrigerant
- cooling
- refrigerant mixture
- refrigeration system
- 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.)
- Expired - Fee Related
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- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 76
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 454
- 239000003507 refrigerant Substances 0.000 claims abstract description 339
- 239000003345 natural gas Substances 0.000 claims abstract description 192
- 239000000203 mixture Substances 0.000 claims abstract description 167
- 238000005057 refrigeration Methods 0.000 claims abstract description 154
- 239000007789 gas Substances 0.000 claims abstract description 123
- 238000000034 method Methods 0.000 claims abstract description 97
- 238000001179 sorption measurement Methods 0.000 claims abstract description 5
- 229930195733 hydrocarbon Natural products 0.000 claims description 139
- 150000002430 hydrocarbons Chemical class 0.000 claims description 139
- 239000007788 liquid Substances 0.000 claims description 133
- 238000001816 cooling Methods 0.000 claims description 110
- 239000004215 Carbon black (E152) Substances 0.000 claims description 71
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 63
- 229910052757 nitrogen Inorganic materials 0.000 claims description 31
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 25
- 230000004087 circulation Effects 0.000 claims description 24
- 238000007710 freezing Methods 0.000 claims description 21
- 230000008014 freezing Effects 0.000 claims description 21
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 18
- 238000003860 storage Methods 0.000 claims description 14
- 229910052724 xenon Inorganic materials 0.000 claims description 14
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 claims description 14
- 239000001569 carbon dioxide Substances 0.000 claims description 13
- 230000006835 compression Effects 0.000 claims description 13
- 238000007906 compression Methods 0.000 claims description 13
- 239000002826 coolant Substances 0.000 claims description 13
- 229910052743 krypton Inorganic materials 0.000 claims description 13
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 13
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 12
- 239000001294 propane Substances 0.000 claims description 10
- 150000001875 compounds Chemical class 0.000 claims description 9
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 7
- 229910052786 argon Inorganic materials 0.000 claims description 6
- 239000001273 butane Substances 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 5
- 239000003915 liquefied petroleum gas Substances 0.000 claims description 5
- 239000012809 cooling fluid Substances 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 2
- 238000010992 reflux Methods 0.000 claims 2
- 235000015110 jellies Nutrition 0.000 claims 1
- 239000008274 jelly Substances 0.000 claims 1
- 230000008569 process Effects 0.000 description 47
- 239000003502 gasoline Substances 0.000 description 27
- 238000002156 mixing Methods 0.000 description 21
- 238000012545 processing Methods 0.000 description 18
- 238000007701 flash-distillation Methods 0.000 description 16
- 239000003795 chemical substances by application Substances 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 14
- 238000004519 manufacturing process Methods 0.000 description 12
- 230000009467 reduction Effects 0.000 description 11
- 239000000446 fuel Substances 0.000 description 10
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 9
- 239000002253 acid Substances 0.000 description 9
- UGCSPKPEHQEOSR-UHFFFAOYSA-N 1,1,2,2-tetrachloro-1,2-difluoroethane Chemical compound FC(Cl)(Cl)C(F)(Cl)Cl UGCSPKPEHQEOSR-UHFFFAOYSA-N 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 230000015572 biosynthetic process Effects 0.000 description 8
- 229920006395 saturated elastomer Polymers 0.000 description 8
- 239000011555 saturated liquid Substances 0.000 description 8
- 238000001704 evaporation Methods 0.000 description 7
- 238000005194 fractionation Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 229910001868 water Inorganic materials 0.000 description 7
- 239000000463 material Substances 0.000 description 6
- GTLACDSXYULKMZ-UHFFFAOYSA-N pentafluoroethane Chemical compound FC(F)C(F)(F)F GTLACDSXYULKMZ-UHFFFAOYSA-N 0.000 description 6
- 229910052734 helium Inorganic materials 0.000 description 5
- 239000001307 helium Substances 0.000 description 5
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 5
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- RWRIWBAIICGTTQ-UHFFFAOYSA-N difluoromethane Chemical compound FCF RWRIWBAIICGTTQ-UHFFFAOYSA-N 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 3
- 229910052753 mercury Inorganic materials 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000000110 cooling liquid Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- FKCNNGCHQHSYCE-UHFFFAOYSA-N difluoromethane;1,1,1,2,2-pentafluoroethane;1,1,1,2-tetrafluoroethane Chemical compound FCF.FCC(F)(F)F.FC(F)C(F)(F)F FKCNNGCHQHSYCE-UHFFFAOYSA-N 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910052754 neon Inorganic materials 0.000 description 2
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 229910052704 radon Inorganic materials 0.000 description 2
- SYUHGPGVQRZVTB-UHFFFAOYSA-N radon atom Chemical compound [Rn] SYUHGPGVQRZVTB-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 238000010257 thawing Methods 0.000 description 2
- INEMUVRCEAELBK-UHFFFAOYSA-N 1,1,1,2-tetrafluoropropane Chemical compound CC(F)C(F)(F)F INEMUVRCEAELBK-UHFFFAOYSA-N 0.000 description 1
- NSGXIBWMJZWTPY-UHFFFAOYSA-N 1,1,1,3,3,3-hexafluoropropane Chemical compound FC(F)(F)CC(F)(F)F NSGXIBWMJZWTPY-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052729 chemical element Inorganic materials 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- -1 ethane Compound Chemical class 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 125000001153 fluoro group Chemical group F* 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000008282 halocarbons Chemical class 0.000 description 1
- 150000005826 halohydrocarbons Chemical class 0.000 description 1
- UKACHOXRXFQJFN-UHFFFAOYSA-N heptafluoropropane Chemical compound FC(F)C(F)(F)C(F)(F)F UKACHOXRXFQJFN-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- MSSNHSVIGIHOJA-UHFFFAOYSA-N pentafluoropropane Chemical compound FC(F)CC(F)(F)F MSSNHSVIGIHOJA-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000010457 zeolite Substances 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
-
- 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"
- F25J1/004—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 flash gas recovery
-
- 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
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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
- F25J1/0062—Light or noble gases, mixtures thereof
-
- 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
- F25J1/0077—Argon
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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
- F25J1/008—Hydrocarbons
- F25J1/0087—Propane; Propylene
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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
- F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
-
- 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
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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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0217—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0219—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
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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
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
- F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
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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
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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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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- Engineering & Computer Science (AREA)
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- 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)
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- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
Disclosed herein is the system and method for forming liquefied natural gas (LNG).The system includes refrigeration system, and it configures to freeze natural gas using the refrigerant mixture for including rare gas.The system is also included from refrigeration system, and it is configured to use natural gas as itself refrigerant with by natural gas adsorption LNG.
Description
The cross reference of related application
The U.S. for the entitled liquefied natural gas formation (LNG FORMATION) submitted for 31st this application claims August in 2012
Submit in state's Provisional Patent Application No. 61/695,592 and on March 30th, 2012 it is entitled low temperature hydrocarbon processing system, device and
Application (the USE OF NOBLE GASES IN LOW TEMPERATURE HYDROCARBON of rare gas in method
PROCESSING SYSTEMS, APPARATUS, AND METHODS) U.S. Provisional Patent Application No. 61/618,290 power
Benefit, is incorporated herein by reference with its whole.
Technical field
Reclaimed present techniques relate generally to hydrocarbon and processing procedure field, and relate more specifically to be formed via process of refrigerastion
The system and method for liquefied natural gas.Specifically there is provided use the refrigerant for including one or more rare gas by natural
Gas formation LNG system and method.
Background technology
This part is intended to introduce the various aspects of this area, and it may be related to the illustrative embodiments of this technology.Phase
Believe that this discussion helps provide the framework for the specific aspect for promoting to more fully understand this technology.It is therefore understood that this part should
Read when from this angle, without recognizing as prior art.
Rely on to use for natural gas processing and liquefied many cryogenic refrigerating systems and include hydrocarbon component and the refrigeration of nitrogen
Agent is to provide external refrigeration.This hydrocarbon component can include methane, ethane, ethene, propane and analog.However, because may
Big heat transfer area is needed to provide the appropriate refrigeration of natural gas, the use of the refrigerant including hydrocarbon component and nitrogen may not be non-
It is often effective.In addition, the combustibility of the hydrocarbon component in refrigerant may increase the danger related to process of refrigerastion.
For natural gas processing and liquefied cryogenic refrigerating system commonly using refrigerant --- such as R-404A synthesized
Or R-410A --- it is used as the replacement including hydrocarbon component and the refrigerant of nitrogen.However, the refrigerant of this synthesis is only suitable only for
For the level of refrigeration higher than about -100 °F.In some cases, relatively low level of refrigeration is probably desired.
Flynn et al. International Patent Application Publication WO/2005/072404 describes a kind of cooling system, and it includes
One refrigerant circulation and second refrigerant circulation, first refrigerant circulation include the first refrigerant, the second refrigerant
Circulation includes the second refrigerant for low temperature component mixture.The disclosure is directed to a kind of cooling system, and it includes the first refrigeration
Agent circulation and second refrigerant circulation, first refrigerant circulation include the first refrigerant, the second refrigerant circulation bag
Include the second refrigerant for non-reactive component.Second refrigerant is free of fluorocarbon, Chlorofluorocarbons and hydrocarbon.Second refrigerant
At least a portion is condensed in second refrigerant circulation.However, the disclosure is not related to including any kind of from freeze cycle
Cooling system.
Relevant information is found in U.S. Patent number 4,533,372,4,923,493,5,265,428,5,062,270,5,
120,338th, 6,053,007 and 5,956,971；U.S. Patent Application Publication No. 2002/0088249,2003/0177785,
2007/0193303、2007/0227185、2008/0034789、2008/0087041、2009/0217701、2009/
0266107th, 2010/0018248,2010/0107684,2010/0186445,2012/0031144,2012/0079852 and
2012/0125043；With International Patent Publication No. WO/2012/015554.Other potentially related information be found in it is international specially
Sharp publication number WO2007/021351；Foglietta, J.H. et al., " Consider Dual Independent Expander
Refrigeration for LNG Production New Methodology May Enable Reducing Cost to
Produce Stranded Gas,”Hydrocarbon Processing,Gulf Publishing Co.,vol.83,no.1,
Pp.39-44 (in January, 2004)；U.S. Patent Application Publication No. US2003/089125；U.S. Patent number 6,412,302；The U.S.
The patent No. 3,162,519；U.S. Patent number 3,323,315；German patent DE19517116 and J.M.Campbell, " Gas
Conditioning and Processing,Vol.2:The Equipment Modules”,8th edition,John
M.Campbell&Company,2001。
The content of the invention
Embodiment provides the system for being used for forming liquefied natural gas (LNG).The system includes refrigeration system, and it is configured
To freeze natural gas using the refrigerant mixture for including rare gas.The system also includes from refrigeration system, its configure so that
With natural gas as itself-refrigerant is with from natural gas adsorption LNG.
Another embodiment provides the method for forming LNG.This method includes freezing in refrigeration systems naturally
Gas, wherein refrigeration system, which are used, includes the refrigerant mixture of rare gas.This method is also included within to liquefy from refrigeration system
Natural gas is to form LNG.
Another embodiment provides the cascade cooling system for forming LNG.Cascading cooling system includes the first system
Cooling system, it is configured to use non-hydrocarbons refrigerant cooled natural gas, wherein the first refrigeration system includes multiple first coolers,
Its configuration allows cooled natural gas with the indirect heat exchange between natural gas and non-hydrocarbons refrigerant.Cascade cooling system
Also the second refrigeration system is included, it is configured to freeze natural gas using the refrigerant mixture for including rare gas, wherein second
Refrigeration system includes multiple second coolers, and it is configured is permitted with the indirect heat exchange between natural gas and refrigerant mixture
Perhaps cooled natural gas.Cascade cooling system further comprises from refrigeration system, and it is configured with from natural gas adsorption LNG, wherein from
Refrigeration system includes multiple expansion valves or hydraulic buckling turbine or its any combination and flash drum.
Brief description
The advantage of this technology is more fully understood by reference to features as discussed above, wherein：
Fig. 1 is the process chart of single-stage refrigerating system；
Fig. 2 is the process chart for the Two-stage refrigerating system for including gasoline economizer；
Fig. 3 is the process chart for the single-stage refrigerating system for including heat exchanger gasoline economizer；
Fig. 4 is the process chart for the cascade cooling system for including the first refrigeration system and the second refrigeration system；
Fig. 5 is the process chart of the expansion refrigeration system controlled for hydrocarbon dew point；
Fig. 6 is the process chart for the NGL expansion refrigeration systems extracted；
Fig. 7 is the process chart of LNG production systems；
Fig. 8 is the process chart for the simplification for cascading cooling system；
Fig. 9 A-B are the more detailed process charts for cascading cooling system；
Figure 10 is the more detailed process chart from refrigeration system；
Figure 11 is the schematic diagram of methane pressure-enthalpy (P-H) figure；With
Figure 12 is the process chart for forming LNG method.
Accompanying drawing is described in detail
In part described in detail below, the embodiment of this technology is described.However, being just described below being directed to
For the embodiment of this technology and the situation of particular use, it is merely intended to as exemplary purpose and simply provided
The descriptions of illustrative embodiments.Therefore, this technology is not limited to specific embodiments described below, but including falling into
All changes, modification and the equivalent form of value in attached spirit and scope by the claims.
Initially, for ease of reference, list this application in some terms used and use within a context they
The meaning.For the situation that terms used herein is not limited below, should provide its people in the related art to
Go out in the most wide restriction of that term, the patent for being such as embodied at least one printed publication or distribution.Moreover, this technology
Do not limited by the use of term as shown below because all equivalent form of values, synonym, new development it is identical with offer or
The term or technology of similar purpose are considered as in the range of present claims.
" sour gas " is the pollutant frequently encountered in natural gas flow.Typically, although other any amount of dirts
Dye thing can also form acid, but these gases include carbon dioxide (CO2) and hydrogen sulfide (H2S).Sour gas is generally by inciting somebody to action
Air-flow and absorbent --- such as amine, it can react with sour gas --- and contact and remove.When absorbent becomes " being rich in " acid
Property gas when, desorption procedure can be used with from absorbent separating acid gas.Then " poor " absorbent is typically recycled for
Further absorb." liquid acid air-flow " is the acid gas stream for being condensed into liquid phase as used herein, it may for example comprise be dissolved in H2S's
CO2And vice versa.
As used herein, referred to " from freezing (from refrigeration, autorefrigeration) " via reduction pressure cooling stream
The process of body.In the case of a liquid, referred to from freezing by evaporative cooling liquid body, the evaporation, which corresponds to, reduces pressure.
More specifically, with withstanding pressure reduction when it passes through throttling arrangement, a part of liquid is flashed as steam.As a result, steam
The saturation temperature of the liquid under reduced pressure is all cooled to both residual liquids.For example, according to implementations described herein,
Natural gas from freezing can by keep natural gas be in its boiling point so as to during evaporating as heat loss natural gas is cold
But carry out.The method also referred to as " is flashed ".
As used herein, " cascade cycle " refers to the system with two or more refrigerants, wherein the second cold system
The first refrigerant condensation that cryogen is relatively warmed up.Therefore, low temperature can by from refrigerant downwards " cascade " to another.Cascade
In every kind of refrigerant multiple freezing levels can be had based on the stage evaporating pressure in gasoline economizer.Because in cascade cycle
In can obtain than lower temperature in unitary system cryogen system, so cascade cycle is considered as compared with unitary system cryogen system
It is beneficial to production LNG.
" closed-loop refrigeration cycle " refers to wherein there is no that refrigerant enters or left circulation in the normal operation period
Kind of refrigeration cycle.
" closed-loop refrigeration system " refers to including the refrigeration system of compression, heat exchange and pressure regulating equipment, wherein refrigerant again
Circulation is withdrawn without continuous deliberate refrigerant.Due to the small leakage loss from system, a small amount of refrigeration is typically needed
Agent is supplemented.
" compressor " or " coolant compressor " includes that any unit, equipment or the dress of the pressure of cold-producing medium stream can be increased
Put.This includes the coolant compressor with single compressed process or step, or the refrigerant pressure with multi-stage compression or step
Contracting machine, specifically in the multi-stage refrigerating agent compressor in single cover or shell.Wait that the cold-producing medium stream for the evaporation compressed can be not
With being provided to coolant compressor under pressure.Some stages of hydrocarbon cooling procedure or step can comprising it is two or more simultaneously
The coolant compressor of connection, series connection or both.The present invention is not by the type of one or more coolant compressors or arrangement or cloth
Office is limited, particularly in any refrigerant loop.
" controlled freeze area " (CFZ) method is the freezing potential for being proposed to utilize the carbon dioxide in low temperature distillation,
Rather than the method for avoiding solid carbon dioxide.In CFZ methods, acid gas components by the carbon dioxide in single column by
Control freezing and thawing are separated by low temperature distillation, and without using freezing suppressant additive.CFZ methods, which are used, has especially inside portion
Divide the low temperature distillation tower of --- such as CFZ parts ---, to handle the solidification and thawing of carbon dioxide.This CFZ part such as simultaneous interpretation
The destilling tower of system does not include filler (packing) or tower tray (tray).But, CFZ parts comprising one or more spray nozzles and
Thaw bowl.Being formed and being fallen in the vapor space of solid carbon dioxide in a distillation column turns into liquid on thaw bowl.The base of formation
All solids are all limited in CFZ parts in sheet.Distillation tower section above and below the CFZ parts of tower is similar to tradition
Low temperature domethanizing column.The more detailed description of CFZ methods is in U.S. Patent number 4,533,372；4,923,493；5,120,338 Hes
Disclosed in 5,265,428.
As used herein, " cooling " refer to reduction and/or decline material temperature and/or interior energy it is for example any suitable
Amount.Cooling can take the photograph including at least about 1 degree Celsius, at least about 5 degrees Celsius, at least about 10 degrees Celsius, at least about 15
The temperature drop of family name's degree, at least about 25 degrees Celsius, at least about 50 degrees Celsius, at least about 100 degrees Celsius and/or similar temperature
It is low.Cooling can use any suitable radiating, such as steam generation, hot water heating, cooling water, air, refrigerant, other works
Skill stream (synthesis) and its combination.One or more sources of cooling can be combined and/or cascade, to reach desired outlet temperature.
Cooling step can use the cooling unit with any suitable device and/or equipment.According to an embodiment, cooling can
With including indirect heat exchange, such as with one or more heat exchangers.Heat exchanger can include any suitable design, example
Such as shell-and-tube, plate and framework, adverse current, following current, the surface of extension and/or analog.In replacement, cooling can use evaporation
(heat of evaporation) is cooled down and/or directly heat exchange, for example, be directly injected to the liquid in technique stream.
" low temperature " refers to about -50 DEG C or less of temperature.
As used herein, term " dethanizer " and " domethanizing column " are referred to for the component in separating natural air-flow
Distillation column or tower.For example, domethanizing column is used to separate methane and other volatile components with ethane and heavier component.Methane fraction
Typically it is recovered as including a small amount of inert gas such as nitrogen, CO2Or the like purified gases.
Term " gas " is convertibly used with " steam ", and is defined as in the gaseous state for being different from liquid or solid-state
Material or mixture of substances.Similarly, term " liquid " mean in be different from gaseous state or solid-state liquid material or
Mixture of substances.
" heat exchanger ", which is widely meant, can be delivered to heat from a medium any equipment of another medium, special
Do not include any structure, such as commonly known as equipment of heat exchanger.Heat exchanger include " direct heat exchanger " and "
Connect heat exchanger ".Therefore, heat exchanger can be plate-and-framework, shell-and-pipe, coil pipe, hairpin structure, core type, core-and-
The known heat exchanger of kettle (core-and-kettle), sleeve pipe or any other type." heat exchanger " may also be referred to
Any post, tower, unit or other arrangements, the arrangement are adapted to allow one or more streams therefrom to pass through, and influence refrigeration
Direct or indirect heat exchange between one or more pipelines of agent and one or more raw material streams.
" hydrocarbon " is the main organic compound including element hydrogen and carbon, but nitrogen, sulphur, oxygen, metal or multiple other elements
Can be to exist in a small amount.As used herein, hydrocarbon is generally referred to as the component found in natural gas, oil or chemical process equipment.
" HFC " or HFC are to include the molecule of H, F and C atom.HFC has H-C and F-C keys and according in species
Carbon atom number C-C keys.Some examples of HFC include fluoroform (CHF3), pentafluoroethane (C2HF5), HFC-134a
(C2H2F4), heptafluoro-propane (C3HF7), HFC-236fa (C3H2F6), pentafluoropropane (C3H3F5) and tetrafluoropropane (C3H4F4), and
The compound of other similar chemical constitutions.
" liquefied natural gas " or " LNG " is commonly known to include the natural gas of high percent-methane.However, LNG can also
Other compounds including trace.Other elements or compound can include, but not limited to ethane, propane, butane, titanium dioxide
Carbon, nitrogen, helium, hydrogen sulfide or its combination, it has been worked upon removing one or more components (for example, helium) or impurity (example
Such as, water and/or heavy hydrocarbon) and then it is condensed into liquid by being cooled under almost atmospheric pressure.
" refrigerant process of mixing " can include, but not limited to the refrigerant using mixing --- i.e. with more than one
The refrigerant of kind of chemical constituent --- single refrigeration system, the refrigerant system of mixing that precools of hydrocarbon and the refrigeration of double mixing
Agent system.Generally, the refrigerant of mixing may include hydrocarbon and/or non-hydrocarbon component.In the refrigerant of mixing typically with conjunction
The example of suitable hydrocarbon component may include, but be not limited to, methane, ethane, ethene, propane, propylene and butane and butylene isomer.
The non-hydrocarbon component usually used in the refrigerant of mixing may include carbon dioxide and nitrogen.The refrigerant process of mixing is used
The refrigerant of at least one blending ingredients, but also can be extraly using the refrigerant of one or more pure components.
" natural gas " refers to the multicomponent gas obtained from crude oil well or from underground gas-bearing formation.The composition and pressure of natural gas
Can significantly it change.Typical natural gas flow includes methane (CH4) it is used as key component, i.e. more than 50 moles of % natural gas
Stream is methane.Natural gas flow can also include ethane (C2H6), hydrocarbon with higher molecular weight is (for example, C3-C20Hydrocarbon), it is one or more acid
Gas (for example, carbon dioxide or hydrogen sulfide) or its any combination.Natural gas can also include a small amount of pollutant, such as water, nitrogen
Gas, iron sulfide, wax, crude oil or its any combination.Natural gas flow can be purified substantially before use in embodiments, so as to
Remove the compound that may act as poisonous substance.
As used herein, " natural gas liquids " (NGL) refers to that its component is the mixed of the hydrocarbon heavy for example typically than ethane
Compound.Some examples of the hydrocarbon component of NGL streams include propane, butane and pentane isomers, benzene, toluene and other aromatic compounds
Thing.
" rare gas " refers to the chemical element of any 18 races for belonging to periodic table.More specifically, rare gas includes
Helium (He), neon (Ne), argon (Ar), krypton (Kr), xenon (Xe) and radon (Rn).Rare gas is characterized by low-down chemistry
Reactivity.
" open loop refrigeration cycle " refers to such kind of refrigeration cycle, wherein the refrigerant used in the normal operation period is at least
The fluid that a part is cooled down from kind of refrigeration cycle.
" open-loop refrigeration system " is the refrigeration system for including compression, heat exchange and decompressor, and wherein refrigerant is recycled,
The refrigerant of a part is continuously withdrawn from recirculation circuit, and extra refrigerant is introduced continuously into recirculation circuit.
" refrigerant component " in refrigeration system will absorb heat by evaporating at relatively low temperatures and pressures, and will be
Pass through condensate drainage heat under higher temperature and pressure.Graphic refrigerant component can include, but not limited to have one to five
Alkane, alkene and the alkynes of carbon atom, nitrogen, chlorinated hydrocabon, fluorinated hydrocarbons, other halogenated hydrocarbons, rare gas and its mixture or group
Compound.
When the quantity or amount on material or its concrete property in use, " substantially " refers to providing material or spy enough
Property be intended to provide effect amount.In some cases, it is allowed to precision runout degree can be according to specific context.
General introduction
Implementations described herein provides hydrocarbon system of processing and method.Such hydrocarbon system of processing can include or profit
With refrigeration system, for example, cascade cooling system.Moreover, according to implementations described herein, refrigeration system is rare using including
The refrigerant mixture of gas.
Hydrocarbon system of processing includes legacy system well known by persons skilled in the art.Hydrocarbon production and processing method includes, but not
It is limited to, freezing natural gas, which is used for NGL extractions, freezing natural gas, is used for hydrocarbon dew point control, freezing natural gas for CO2Removal, liquid
Liquefied oil gas (LPG) production inventory, the condensation of backflow in dethanizer/domethanizing column and natural gas liquefaction are to produce LNG.
Although it is cascade that multiple kind of refrigeration cycle, which have been used to process the circulation used in hydrocarbon, LNG liquefying plants,
Circulation, it is warm to liquefaction with the temperature for reducing gas progressively using multiple one-component refrigerants in the heat exchanger installed
Degree.Another circulation used in LNG liquefying plants is multiple group sub-refrigerating circulation, and it uses many in specially designed exchanger
Component refrigerants.In addition, another circulation used in LNG liquefying plants is expander circulation, it is with corresponding temperature
Reduction expansion gas is from material pressure to low pressure.NG Liquefaction cycle can also use the change or combination that these three are circulated.
LNG is prepared by refrigeration and liquefaction technology by unstripped gas.Optional step includes condensate removal, CO2Remove, take off
Water, mercury removal, nitrogen stripping (stripping), H2S removals etc..After liquefaction, LNG can be stored or be fed to gas pipeline
For selling or using.Traditional liquifying method may include：The mix refrigerant of APCI propane pre-coolings but；C3MR；DUAL MR；
Cascade optimal Phillips；The refrigerant of the single mixing of Prico；The refrigerant of the double pressure mixing of TEAL；Linde/Statoil
Multi-fluid is cascaded；The refrigerant of the double mixing of Axens, DMR；With Shell methods C3MR and DMR.
Carbon dioxide is removed, i.e., by methane and lighter gas and CO2Separated with heavier gas, low-temperature treatment can be used real
It is existing, such as from controlled freeze area technology obtained by Exxon Mobil Corporation.
Although on discussing method described herein and system, this method and system by natural gas adsorption LNG
Available for various other purposes.For example, method described herein and system can be used for cooled natural gas to be controlled for hydrocarbon dew point, enter
Row natural gas liquids (NGL) are extracted, and methane and lighter gas are separated with carbon dioxide and heavier gas, hydrocarbon is prepared for LPG
Backflow in production or condensation dethanizer and/or domethanizing column, etc..
Refrigerant
The refrigerant utilized according to implementations described herein can be one or more one-component refrigerants, or bag
Include the refrigerant mixture of various ingredients.Refrigerant can include methane, ethane, ethene, propane, butane and nitrogen or its group
Close.In implementations described herein, the refrigerant in one or more cooling stages, which is used, includes rare gas and rare
The nonflammable material of admixture of gas.Refrigerant can be inputted or stored by scene, or alternatively, some components of refrigerant
It can be prepared in situ typically via the still-process integrated with hydrocarbon system of processing.The refrigerant of exemplary mixing is in U.S. Patent number
Disclosed in 6,530,240.
Commercially available refrigerant including fluorocarbon (FC) or HFC (HFC) is used in various applications, including
Ammonia, sulfur dioxide or halo hydrocarbon coolant are also such.Exemplary refrigerant is from DuPont Corporation commercially availables
, includingRefrigerant family,Refrigerant family,Refrigerant family andRefrigerant family.
Multi-component refrigrant is commercially available.For example, R-401A is R-32, R-152a and R-124 HCFC mixtures.
R-404A is 52wt.%R-143a, 44wt.%R-125 and 4wt.%R-134a HFC mixtures.R-406A is 55wt.%R-
22nd, 4wt.%R-600a and 41wt.%R-142b mixture.R-407A be 20wt.%R-32,40wt.%R-125 and
40wt.%R-134a HFC mixtures.R-407C is R-32, R-125 and R-134a HFC mixture.R-408A is R-
22nd, R-125 and R-143a HCFC mixtures.R-409A is R-22, R-124 and R-142b HCFC mixtures.R-410A is
R-32 and R-125 mixture.R-500 is 73.8wt.%R-12 and 26.2wt.%R-152a mixture.R-502 is R-22
With R-115 mixture.
In implementations described herein, the refrigerant in one or more cooling stages can also include rare gas
Body or rare gas mixture.Six kinds of rare gas occurred naturally are helium (He), neon (Ne), argon (Ar), krypton (Kr), xenon
And radon (Rn) (Xe).Rare gas can be used alone or is applied in combination with other rare gas, or with other refrigerant component groups
Conjunction is used.In some embodiments, the rare gas as refrigerant is xenon, krypton, argon or its combination.
Because rare gas is nonflammable, they reduce the danger of processing refrigerant.In addition, because rare gas
Body is present in air, and easily collects, and any rare gas refrigerant for escaping refrigeration system is recyclable.If moreover,
It is discharged into environment, rare gas does not have any ozone depletion potential or greenhouse temperature increasing potential.
Rare gas refrigerant can be provided less than about -50 °F or less than about -100 °F or less than about -120 °
F or from about -50 °F to about -162 °F or from about -50 °F to about -244 °F or from about -50 °F to about -
303 °F of cooling.In multistage refrigerating plant, freezed in stage that can be below using rare gas refrigerant with realizing than hydrocarbon
The deeper cooling that agent is provided, such as less than about -50 °F or less than about -100 °F or less than about -120 °F or from big
About -50 °F to about -162 °F or from about -90 °F to about -162 °F or from about -100 °F to about -162 °F or from
About -120 °F to about -162 °F or from about -50 °F to about -244 °F or from about -90 °F to about -244 °F or
From about -100 °F to about -244 °F or from about -120 °F to about -244 °F or from about -50 °F to about -303 °
F or from about -90 °F to about -303 °F or from about -100 °F to about -303 °F or from about -120 °F to about -
303°F。
In multiple embodiments, any refrigeration system that any number of different types of hydrocarbon system of processing can be with text description
It is used together.In addition, refrigeration system described herein can utilize any refrigerant described above.
Refrigeration system
Hydrocarbon system and method generally include the refrigeration system using mechanical refrigeration, valve expansion, turbine expansion etc..Mechanical refrigeration
Typically comprise compressibility and absorption system, such as ammonia absorption system.Compressibility is used in gas processing industry, is used for
Multiple processes.For example, compressibility can be used for freezing natural gas to be extracted for NGL, freezing natural gas is used for hydrocarbon dew point control,
The condensation of backflow in LPG production inventories, dethanizer or domethanizing column, natural gas liquefaction are to produce LNG or similar application.And
And, it can utilize the flammable with other refrigeration of replacement of the reduction of rare gas inherently using other commercialization process of refrigeration
Agent, such as ammonia.
Fig. 1 is the process chart of single-stage refrigerating system 100.In multiple embodiments, single-stage refrigerating system 100 is utilized
Refrigerant mixture including rare gas.Single-stage refrigerating system 100 include expansion valve 102, cooler 104, compressor 106,
Condenser 108 and storage tank 110.Saturated liquid refrigerant 112 can flow to expansion valve 102 from storage tank 110, and can constant enthalpy
(isenthalpically) expansion valve 102 is expanded through.During expansion, some vaporizations occur, and formation includes both steam and liquid
Freezing refrigerant mixture 114.Refrigerant mixture 114 can be than technique stream 116, and --- such as natural gas --- is treated
Enter cooler 104 under the temperature lower temperature being cooled to, it is also referred to as evaporator.Technique stream 116 flows through cooler 104
And with the exchanged heat of refrigerant mixture 114.With technique stream 116 and the exchanged heat of refrigerant mixture 114, technique stream 116 is cold
But, while refrigerant mixture 114 can at least partly evaporate, saturated vapor refrigerant 118 is formed.
Leave after cooler 104, saturated vapor refrigerant 118 and any remaining liquid refrigerant, in compressor 106
It is interior to be compressed, and then flow into condenser 108.Within condenser 108, saturated vapor refrigerant 118 is converted into saturation
Or little too cold liquid refrigerant 120.Liquid refrigerant 120 and then can flow to storage tank 110 from condenser 108.Storage tank
110, also referred to as surge tank or receiver can serve as the reservoir (reservoir) of liquid refrigerant 120.Liquid refrigerating
Agent 120 can be stored in storage tank 110 before expanding through expansion valve 102 as saturated liquid refrigerant 112.
It should be understood that Fig. 1 process chart is not intended to show that single-stage refrigerating system 100 includes all portions shown in Fig. 1
Part.Moreover, according to the details of specific implementation, single-stage refrigerating system 100 can include any amount of extra not shown in Fig. 1
Part.For example, in some embodiments, refrigeration system may include two or more compression stages.In addition, as further
Discussed on Fig. 2, refrigeration system 100 can include gasoline economizer.
Fig. 2 is the process chart for the Two-stage refrigerating system 200 for including gasoline economizer 202.The entry of identical numbering such as on
Described by Fig. 1.Gasoline economizer 202 can be any the setting of utilizing of compressor horsepower for the cooler work (duty) that reduction is provided
Standby or process reform.Traditional gasoline economizer 202 includes, for example, flash tank and heat exchange gasoline economizer.
As shown in Figure 2, expansion valve 102 can be expanded through to steam by leaving the saturated liquid refrigerant 112 of storage tank 110
The intermediate pressure that can be separated with liquid.Expansion valve 102 can be used for the downstream temperature and pressure of control saturated liquid refrigerant 112
Power.For example, as saturated liquid refrigerant 112 is flashed through expansion valve 102, vapor refrigerant 204 and liquid refrigerant 206 exist
Produced under the pressure and temperature lower than saturated liquid refrigerant 112.Vapor refrigerant 204 and liquid refrigerant 206 and then can be with
Flow into gasoline economizer 202.In multiple embodiments, gasoline economizer 202 is to realize 206 points of vapor refrigerant 204 and liquid refrigerant
From flash tank.Vapor refrigerant 204 can flow to intermediate pressure compressor section, can be with leaving in this vapor refrigerant 204
The saturated vapor refrigerant 118 of one compressor 210 is combined, and forms the saturated vapor refrigerant 208 of mixing.The saturated vapor of mixing
Refrigerant 208 may then flow into the second compressor 212.
Liquid refrigerant 206 can expand through the second expansion valve 214 from the constant enthalpy of gasoline economizer 202.During expansion, some vapour
Change may occur in which, being formed includes steam and the refrigerant mixture 216 both liquid, reduction temperature and pressure.Refrigerant mixture
216 can have the content liquid higher than refrigerant mixture in the system without gasoline economizer.Higher content liquid can subtract
Small refrigerant circulation speed and/or the power utilization for reducing the first compressor 210.
Refrigerant mixture 216 enters cooler 104 under the temperature lower temperature arrived more to be cooled than technique stream 116,
It is also referred to as evaporator.Such as discussed above on Fig. 1, technique stream 116 is cooled within cooler 104.In addition, as closed
Discussed above in Fig. 1, saturated vapor refrigerant 118 flows through compressor 210 and 212 and condenser 108, and the liquid of gained
Refrigerant 120 is stored in storage tank 110.
It should be understood that Fig. 2 process chart is not intended to show that Two-stage refrigerating system 200 includes all portions shown in Fig. 2
Part.Moreover, according to the details of specific implementation, Two-stage refrigerating system 200 can include any amount of extra not shown in Fig. 2
Part.For example, Two-stage refrigerating system 200 can be including other classes not shown in any amount of extra gasoline economizer or Fig. 2
The equipment of type.In addition, gasoline economizer 202 can be heat exchange gasoline economizer rather than flash tank.Heat exchange gasoline economizer can be used for
Reduce kind of refrigeration cycle speed and reduce compressor horsepower and utilize.
In some embodiments, Two-stage refrigerating system 200 includes more than one gasoline economizer 202, and more than two
Compressor 210 and 212.For example, Two-stage refrigerating system 200 can include two gasoline economizers and three compressors.Generally, if
Refrigeration system 200 includes the gasoline economizer of X quantity, and refrigeration system 200 will include the compressor of X+1 quantity.With multiple gasoline economizers
Such refrigeration system 200 can form a part for cascade refrigeration system.
Fig. 3 is the process chart for the single-stage refrigerating system 300 for including heat exchanger gasoline economizer 302.The bar of identical numbering
Mesh is as described in Figure 1 on.As shown in figure 3, expansion can be expanded through by leaving the saturated liquid refrigerant 112 of storage tank 110
Valve 102 can produce refrigerant mixture 114 to steam and liquid by separated intermediate pressure.Refrigerant mixture 114 can be with
Cooler 104 is flowed under the temperature lower temperature arrived more to be cooled than technique stream 116.It is such as discussed above on Fig. 1, technique
Stream 116 can be cooled in cooler 104.
Saturated vapor refrigerant 118 can flow through heat exchanger gasoline economizer 302 from cooler 104.Cold low pressure saturation is steamed
Vapour refrigerant 118 can be used for being subcooled saturated liquid refrigerant 112 in heat exchanger gasoline economizer 302.Such as begged on more than Fig. 1
Opinion, leave the superheated vapor refrigerant 304 of heat exchanger gasoline economizer 302 and then compressor 106 and condenser can be flowed through
108, and the liquid refrigerant 120 of gained is storable in storage tank 110.
It should be understood that Fig. 3 process chart is not intended to show that single-stage refrigerating system 300 includes all portions shown in Fig. 3
Part.Moreover, according to the details of specific implementation, single-stage refrigerating system 300 can include any amount of extra not shown in Fig. 3
Part.
Fig. 4 is the technological process for the cascade cooling system 400 for including the first refrigeration system 402 and the second refrigeration system 404
Figure.In multiple embodiments, the first refrigeration system 402, which is utilized, includes the refrigerant of rare gas such as xenon or krypton, and second
Refrigeration system 404 can utilize different rare gas refrigerant, fluorocarbon refrigerants or hydrocarbon coolant.Refrigeration system
402 or 404 it is any in refrigerant can include mixture.Cascade cooling system 400 compares refrigeration system available for expectation
100th, the situation of the cooling of 200 or 300 higher degrees provided.Cascading cooling system 400 can be in low-down temperature for example
Cooling is provided at less than -40 DEG C.
In the first refrigeration system 402, liquid refrigerant stream 406 can flow through the first expansion valve 410 and from storage tank 408
One heat exchanger 412, it cools down product stream 413.The vapor/liquid stream of gained is separated in the first flash drum 414.A part
Liquid refrigerant stream 406 can flow directly into the first flash drum 414 via by-passing valve 416, and this can be used for the first flash drum of control
The temperature of liquid in 414, and the cooling in first heat exchanger 412 amount.
Liquid refrigerant stream 418 can flow through the second expansion valve 420 from the first flash drum 414, and flash into the second heat
Exchanger 422, it can be used for further cooling product stream 413.Vapor refrigerant stream 426 obtained by the supply of gas reservoir 424 is arrived
First stage compressor 428.The intermediate pressure vapor refrigerant stream 430 of gained with from the steam-refrigerated of the first flash drum 414
Agent stream 432 is combined, and the stream combined is supplied to second stage compressor 434.High pressure from second stage compressor 434
Steam stream 436 passes through condenser 438, and it can use the cooling from the second refrigeration system 404.Especially, condenser 438 can
To produce liquid refrigerant stream using the cooling high pressure steam flow 436 of low-temperature refrigerant stream 440 from the second refrigeration system 404
406.The liquid refrigerant stream 406 for carrying out condenser 438 is then store in storage tank 408.Control valve 442 can be used for control low temperature
Cold-producing medium stream 440 flows through condenser 438.The vapor refrigerant stream 444 of gained returns to the second refrigeration system from condenser 438
404。
In the second refrigeration system 404, liquid refrigerant stream 448 can flow through heat exchanger 452 from storage tank 450, described
Heat exchanger 452 is configured with via the cooling liquid cold-producing medium stream 448 of refrigeration system 454.The low-temperature refrigerant stream 456 of gained can be with
The first expansion valve 458 and first heat exchanger 460 are flowed through, it cools down product stream 413.The vapor/liquid cold-producing medium stream of gained exists
Separated in first flash drum 462.The low-temperature refrigerant stream 456 of a part can flow directly into the first flash distillation via by-passing valve 464
Drum 462, the temperature of this liquid that can be used in the first flash drum 462 of control, and cooling in first heat exchanger 460
Amount.
Liquid refrigerant stream 466 can flow through the second expansion valve 468 from the first flash drum 462, and flash into the second heat
Exchanger 470, it can be used for further cooling product stream 413.The vapor/liquid cold-producing medium stream of gained is in the second flash drum 472
Middle separation.The liquid refrigerant stream 466 of a part can flow directly into the second flash drum 472 via by-passing valve 474, and this can be used for
Control the temperature of the liquid in the second flash drum 472, and the cooling in second heat exchanger 470 amount.
Liquid refrigerant stream 476 can flow through the 3rd expansion valve 478 from the second flash drum 472, and flash into the 3rd heat
Exchanger 480, it can be used for further cooling product stream 413.Vapor refrigerant stream 484 obtained by the supply of gas reservoir 482 is arrived
First stage compressor 486.The intermediate pressure vapor refrigerant stream 488 of gained with from the steam-refrigerated of the second flash drum 472
Agent stream 490 is combined, and the stream combined is supplied to second stage compressor 492.The high-pressure vapor refrigerant stream 494 of gained with
Vapor refrigerant mixture 496 from the first flash drum 462 is combined, and the stream combined is supplied to phase III compressor
497.The high-pressure vapor refrigerant stream 498 of gained flows through heat exchanger 499, and the high-pressure vapor refrigerant stream 498 leads to wherein
Crossing can be further cooled with cooling water indirect heat exchange.The liquid refrigerant stream 448 of gained may then flow into storage tank 450.
It should be understood that Fig. 4 process chart is not intended to show to cascade all portions that cooling system 400 includes showing in Fig. 4
Part.Moreover, according to the details of specific implementation, cascade cooling system 400 can include any amount of extra not shown in Fig. 4
Part.
Fig. 5 is the process chart of the expansion refrigeration system 500 controlled for hydrocarbon dew point.Heavy hydrocarbon in pipeline in natural gas
Such as C3-C6Condensation manifold pressure can be caused to increase, and processing equipment power utilization increase.Therefore, in order to prevent this
Condensation is planted, the reduction hydrocarbon dew point of expansion refrigeration system 500 can be used.
As shown in Figure 5, the natural gas feedstream 502 of dehydration can be with inflow gas/gas heat-exchanger 504.Gas/
In gas heat-exchanger 504, the natural gas feedstream 502 of dehydration can by with the indirect heat exchange of cryogenic natural gas stream 506 by
Cooling.The natural gas flow 508 of gained can flow into the first separator 510, and it can remove same amount of heavy from natural gas flow 508
Hydrocarbon 512.In multiple embodiments, the dew point that heavy hydrocarbon 512 reduces natural gas flow 508 is removed from natural gas flow 508.Remove
Heavy hydrocarbon 512 can flow out expansion refrigeration system 500 by first outlet valve 514.For example, heavy hydrocarbon 512 can be from swell refrigeration system
System 500 flows to stabilizer (not shown).
Natural gas flow 508 may then flow into expander 516.In multiple embodiments, expander 516 is turbine expansion
Device, it is radial outward flow turbine or axial turbine.Expansion of the natural gas flow 508 in expander 516 can be provided for driving
The energy of dynamic compressor 518, the compressor 518 is connected to expander 516 via axle (shaft) 520.
The cryogenic natural gas stream 506 of gained can flow into the second separator 522 from expander 516, and it can be from low temperature day
Right air-flow 506 removes any remaining heavy hydrocarbon 512.In multiple embodiments, heavy hydrocarbon 512 is removed from cryogenic natural gas stream 506
It reduce further the dew point of cryogenic natural gas stream 506.Then the heavy hydrocarbon 512 of removal can be flowed out swollen by second outlet valve 524
Swollen refrigeration system 500.
Cryogenic natural gas stream 506 can flow to gas/gas heat exchangers 504 from the second separator 522, and it can increase
The temperature of cryogenic natural gas stream 506, produces high-temperature natural gas stream 526.Then high-temperature natural gas stream 526 can flow through compressor
518, it can return to the pressure of natural gas flow 526 acceptable acid gas pressure.Finally, the dew point natural gas of reduction
Then stream 528 can flow out expansion refrigeration system 500.
In embodiments, for example, can be used for increasing further to process using the cooling system of rare gas refrigerant
Cooling.This cooling can by cryogenic natural gas stream 506, the placed upstream heat exchanger of the second separator 522 530 it is real
Apply.Refrigerant liquid 532 can pass through expansion valve 534 by the flash distillation of cooler 530.Then the refrigerant vapour 536 of gained can return
Return to refrigerant system.Cooling can allow the condensable hydrocarbons for removing much higher amount, such as C3S and Geng Gao.Moreover, at some
In embodiment, heat exchanger 530 is placed on the upstream of expander 516, and separator is located at heat exchanger 530 and expander
Between 516, to prevent liquid flow from entering expander 516.
It should be understood that Fig. 5 process chart is not intended to show that expansion refrigeration system 500 includes all portions shown in Fig. 5
Part.Moreover, according to the details of specific implementation, expansion refrigeration system 500 can include any amount of extra not shown in Fig. 5
Part.
Fig. 6 is the process chart for the NGL expansion refrigeration systems 600 extracted.In multiple embodiments, it can implement
NGL is extracted to reclaim NGL, and it includes any amount of different heavy hydrocarbon from natural gas flow.Due to NGL be often it is larger
The fact that value, in order to heat the purpose of fuel different from gaseous state, it can be desired that NGL, which is extracted,.
Dry natural gas raw material stream 602 can be from dewatering system inflow gas/gas heat-exchanger 604.In gas/gas
In heat exchanger 604, can by with the indirect heat exchange of cryogenic natural gas stream 606 come cool drying natural gas feedstream 602.Gained
Natural gas flow 608 can flow into separator 610, it can remove a part of NGL612 from natural gas flow 608.Remove
NGL612 can flow into dethanizer or domethanizing column 614 from separator 610.
Natural gas flow 608 may then flow into expander 616.In multiple embodiments, expander 616 is turbine expansion
Device.Expansion of the natural gas flow 608 in expander 616 can provide the energy for driving compressor 618, the compressor
618 are connected to expander 616 via axle 620.In addition, can reduce naturally through joule-Thomson valve 622 via adiabatic expansion
The temperature of air-flow 608.
The cryogenic natural gas stream 606 of gained can flow into dethanizer or domethanizing column 614 from expander 616.In de- second
In alkane tower or domethanizing column 614, NGL can be separated with natural gas flow 606, and de- second can be flowed out as NGL product streams 624
Alkane tower or domethanizing column 614.Then NGL product streams 624 can pump out via pump 626 from expansion refrigeration system 600.
Dethanizer or domethanizing column 614 may be coupled to heat exchanger 628.In some embodiments, heat exchanger
628 be reboiler 628, and it can be used for coming from dethanizer or demethanation via the indirect heat exchange heating in high temperature fluid 632
The tower base stream (bottoms stream) 630 of a part for tower 614.Then the tower base stream 630 of heating can reinject de- second
Alkane tower or domethanizing column 614.
The separation of NGL product streams 624 and natural gas flow 606 may cause to produce in dethanizer or domethanizing column 614
Cryogenic natural gas stream, it can flow out dethanizer or domethanizing column 614 as overhead stream (overhead stream) 634.
Overhead stream 634 can be with inflow heat exchanger 636, and it can be by indirect with the refrigerant mixture 638 including rare gas
Heat exchange reduces the temperature of overhead stream 634.The reduction of temperature can cause some steam to condense.Overhead stream 634 and then can be with
Separated in separation container 640, to produce cryogenic natural gas stream 606 and liquid bottoms stream 642.Tower base stream 642 can be via
Pump 644 is pumped back to dethanizer or domethanizing column 614, forms recirculation flow.
Then cryogenic natural gas stream 606 can flow through gas/gas heat exchangers 604.The temperature of cryogenic natural gas stream 506
It can be raised in gas/gas heat exchangers 604, produce high-temperature natural gas stream 646.Then high-temperature natural gas stream 646 can flow
Overcompression machine 618, it can increase the pressure of natural gas flow 646.In some embodiments, high-temperature natural gas stream 646 also flows
The second compressor 648 is crossed, it can increase the pressure of natural gas flow 646 to acceptable acid gas pressure.Gas product
Then stream 650 can flow out expansion refrigeration system 600.
It should be understood that Fig. 6 process chart is not intended to show that expansion refrigeration system 600 includes all portions shown in Fig. 6
Part.Moreover, according to the details of specific implementation, expansion refrigeration system 600 can include any amount of extra not shown in Fig. 6
Part.
Fig. 7 is the process chart of LNG production systems 700.As shown in Figure 7, using multiple different refrigeration systems,
LNG702 can be produced from natural gas flow 704.As shown in Figure 7, a part of natural gas flow 704 can produce system entering LNG
Separated before system 700 from natural gas flow 704, and may be used as fuel gas stream 706.Remaining natural gas flow 704 can flow
Enter initial gas processing system 708.In gas processing system 708, natural gas flow 704 can be purified and cool down.For example,
Rare gas refrigerant, such as the refrigerant mixture cooled natural gas stream 704 including one or more rare gas can be used.
For example, heavy hydrocarbon 710 can be removed from natural gas flow 706, and available for the production gasoline 712 in heavy hydrocarbon system of processing 714.
In addition, any remaining natural gas 716 separated during production gasoline 712 with heavy hydrocarbon 710 may return to natural gas flow 704.
Natural gas flow 704 can be converted into LNG702 in low temperature heat exchanger 718.In some embodiments, from mixed
The cold-producing medium stream 720 of the mixing of the refrigeration system 722 of conjunction is used for the cooled natural gas stream 704 in low temperature heat exchanger 718.According to
Implementations described herein, the cold-producing medium stream 720 of mixing is to include the refrigerant mixture of one or more rare gas.
In other embodiment, the hydrocarbon coolant stream (not shown) from hydrocarbon refrigeration system 724 is used for cold in low temperature heat exchanger 718
But natural gas flow 704, to produce LNG702.
It should be understood that Fig. 7 process chart is not intended to show that LNG production systems 700 include all portions shown in Fig. 7
Part.Moreover, according to the details of specific implementation, LNG production systems 700 can include any amount of extra not shown in Fig. 7
Part.For example, any amount of optional refrigeration system can also be used for producing LNG702 from natural gas flow 704.In addition, any number
The different refrigeration systems of amount can be applied in combination to produce LNG702.
Cascade cooling system for producing liquefied natural gas
Fig. 8 is the process chart for the simplification for cascading cooling system 800.Cooling system 800 is cascaded to can be used for from former natural
Gas 804 produces LNG802.The entrance washer 806 that raw natural gas 804 can be flowed into cascade cooling system 800.Entrance is washed
Device 806 can remove unwanted particle from raw natural gas 804.As natural gas enters cascade cooling system 800, entrance meter
Scale 808 can monitor the amount and characteristic of natural gas.Natural gas can be by amine processor 810, and it can be removed from natural gas
Hydrogen sulfide, carbon dioxide and other unwanted gases, and can in the heat exchanger 812 via with propane or any other
Suitable cooling agent indirect heat exchange and be frozen.
Natural gas can flow through the first dewaterer 814, and it can be from natural gas via gravity based separation process removal water
816.The water 816 of removal can be exported from cascade cooling system 800.Then natural gas can flow to the second dewaterer 818, and it can
To remove any remaining water from natural gas.Second dewaterer 818 can be for example, molecular sieve bed or zeolite beds.
Can include molecular sieve bed mercury removal system 820 can from natural gas removal of mercury.In addition, dry gas filter
822, such as pleat paper filter can remove any residual particles from natural gas.
The natural gas 823 of purifying can be sent to the first ice chest 824 in refrigeration system 826 from dry gas filter 822.
In this example, the first ice chest 824 can play both heat exchanger and flash drum.However, in other implementations, can make
Use single flash drum, the gasoline economizer 202 for example discussed on Fig. 2.Therefore, the first ice chest 824 can freeze via with first
The indirect heat exchange of agent composition 828 carrys out cooled natural gas.First refrigerant mixture 828 can be traditional refrigerant, example
Such as HFC or propane.In addition, the first ice chest 824 can serve as steam-liquid separator, the first refrigerant mixture of separation is steaming
Vapour refrigerant mixture 830 and liquid refrigerant mixture.Vapor refrigerant mixture 830 can be via through expansion valve 832
The first refrigerant mixture 828 flash distillation and produce.Expansion valve 832 can throttle the first refrigerant mixture 828 to reduce
The pressure and temperature of first refrigerant mixture 828, causes the flash distillation of the first refrigerant mixture 828.In some embodiments
In, the first refrigerant mixture 830 can be completely vaporised, and therefore, no liquid refrigerant mixture may reside in
In first ice chest 824.
First refrigerant mixture 828 continuously can be recycled and recycled in refrigeration system 826.For example, first
Refrigerant mixture 828 is passed through after the first ice chest 824, and the vapor refrigerant mixture 830 of gained is can be by the first gas turbine
Compressed in the high pressure compressor 834 of 836 energy supplies.High pressure compressor 834 can be energized by gas only turbine, for example, passing through
It is placed on common or connection axle, or can be energized by motor.Vapor refrigerant mixture 830 is then cold first
Liquid refrigerant mixture 828 is condensed into condenser 838.Then liquid refrigerant mixture 828 can be stored in surge tank
In 840, liquid refrigerant mixture can flow back into the first ice chest 824 to terminate cooling circulation from surge tank 840.
Second refrigerant mixture 842 can also be used for the natural gas 823 that further cooling is purified in the second ice chest 844.
In this example, the second ice chest 834 is handed over via with the indirect thermal of second refrigerant mixture 842 including at least one rare gas
Bring the natural gas 823 of further cooling purifying.In addition, the second ice chest 844 can serve as steam-liquid separator, separation the
Two refrigerant mixtures 842 are vapor refrigerant mixture 846 and liquid refrigerant mixture.Vapor refrigerant mixture 846
It can be produced via the flash distillation of the second refrigerant mixture 842 through expansion valve 848.Expansion valve 848 can throttle the second refrigeration
Agent composition 842 causes the sudden strain of a muscle of second refrigerant mixture 842 to reduce the pressure and temperature of second refrigerant mixture 842
Steam.In some embodiments, second refrigerant mixture 842 can be completely vaporised, and therefore, without liquid refrigerant
Mixture may reside in the second ice chest 844.
Leaving the vapor refrigerant mixture 846 of the gained of the second ice chest 844 can energize by the second gas turbine 852
Low pressure compressor 850 in compressed, produce compression refrigerant mixture 85.Low pressure compressor 850 can be by gas only
Turbine is energized, for example, by being placed on common or connection axle, or can be energized by motor.The refrigerant of compression
Mixture 854 then can be in low-temperature condenser 856 --- such as ammonia cooler --- be inside condensed to produce second refrigerant
Mixture 842.Second refrigerant mixture 842 can be stored in surge tank 858, and second refrigerant mixture 842 can be from
Surge tank 858 flow back into the second ice chest 844 to terminate cooling circulation.
After natural gas 823 has been cooled down in ice chest 824 and 844, natural gas 823 can be entered from refrigeration system 860
One step cools down and liquefied, and produces LNG802.In some embodiments, (do not show including a series of expansion valves from refrigeration system 860
Go out) and flash drum (not shown), it is gradually lowered the temperature and pressure of natural gas, until natural gas is under atmospheric pressure or close
Atmospheric pressure reaches liquid.In addition, flowing into from before refrigeration system 860, natural gas 823 can flow through high pressure nitrogen rejection facility
(NRU) (not shown).NRU can remove some parts of nitrogen from natural gas 823, and therefore, it can allow to use to contain
There is the gas of high percentage nitrogen.
Natural gas steam can also be produced from refrigeration system 860, it can be used as fuel 862.Fuel 862 can be in outflow cascade
Compressed before cooling system 800 in the compressor 864 energized by the 3rd gas turbine 866.According to the need to fuel 862
Ask, most natural gas steam can be reconfigured with the natural gas 823 of initial purification, and return in system be used for into
One step is processed.
The LNG802 of generation can be stored in LNG tank 868 before cascade cooling system 800 is sent out.Gas can
It is discharged out and is pumped back to via the first pump 870 from refrigeration system 860 from LNG tank 868.In addition, being filled on charging appliance
The gas 872 separated during LNG802 with LNG802 is carried, for example, can be pumped back into via the second pump 874 from refrigeration system
860。
It should be understood that Fig. 8 process chart is not intended to show to cascade all portions that cooling system 800 includes showing in Fig. 8
Part.Moreover, according to the details of specific implementation, cascade cooling system 800 can include any amount of extra not shown in Fig. 8
Part.
Fig. 9 A-B are the more detailed process charts for cascading cooling system 900.It can be used for cascade cooling system 900
Produce LNG cascade, open loop liquefaction system.Cascading cooling system 900 can be in low temperature --- for example, less than about 0 °F or
Less than about -20 °F or less than about -40 °F --- it is lower to operate.In addition, cascade cooling system 900 can use more than one
Refrigerant and refrigeration is provided at multiple temperatures.
As shown in Figure 9 A, cascade cooling system 900 can include the first refrigeration system 902, and it can utilize non-hydrocarbons system
Cryogen such as HFC, for example, R-404A or R-410a.As shown in Figure 9 B, cascade cooling system 900 can also include the second system
Cooling system 904, the refrigerant that it, which can be utilized, includes at least one rare gas --- such as xenon, krypton, argon or its combination ---
Mixture.
Figure 10 is the more detailed process chart from refrigeration system 1000.As discussed further below, from freezing system
System 1000 can be located at the downstream of cascade cooling system 900.
The pipe joint 910 that natural gas flow 908 can be flowed into cascade cooling system 900.Pipe joint 910 can be configured
With the natural gas flow that separated natural gas flow 908 is two separation.One natural gas flow 914 can flow into another pipe joint
912, and another natural gas flow 916 can be flowed into from refrigeration system 1000.
In pipe joint 912, natural gas flow 914 can with from the natural gas steam stream 1066 from refrigeration system 1000
Combination.The natural gas flow 918 of gained may then flow into the first refrigeration system 902, prepare to be used for cooled natural gas stream 918.My god
Right air-flow 918 can by through a series of heat exchangers 920,922,924 and 926 in the first refrigeration system 902 and it is cold
But.Heat exchanger 920,922,924 and 926 can also be referred to as evaporator, cooler or ice chest.Natural gas flow 918 can be
It is cooled in each of heat exchanger 920,922,924 and 926 by the non-hydrocarbons indirect heat exchange with circulation.
Non-hydrocarbons refrigerant can be HFC, such as R-404A or R-410A, or any other is adapted to the non-hydrocarbons refrigerant of type.
Non-hydrocarbons refrigerant can be continuously circulated through the first refrigeration system 902, its can continuously prepare be used for into
Enter the non-hydrocarbons refrigerant of each of heat exchanger 920,922,924 and 926.Non-hydrocarbons refrigerant can be used as steam nonhydrocarbon
Class refrigerant leaves first heat exchanger 920 via pipeline 928.Steam non-hydrocarbons refrigerant can with pipe joint 930
Extra steam non-hydrocarbons refrigerant compositions.Steam non-hydrocarbons refrigerant then passes through compressor 932 to increase steam non-hydrocarbons
The pressure of refrigerant, produces the steam non-hydrocarbons refrigerant of overheat.Superheated steam non-hydrocarbons cold-producing medium stream crosses condenser 934, its
Superheated steam non-hydrocarbons refrigerant can be cooled down and condensed, liquid non-hydrocarbons refrigerant is produced.
Liquid non-hydrocarbons refrigerant can flow through expansion valve 935, and it reduces the temperature and pressure of liquid non-hydrocarbons refrigerant.
This can cause the flash distillation of liquid non-hydrocarbons refrigerant, produce the mixing of liquid non-hydrocarbons refrigerant and steam non-hydrocarbons refrigerant
Thing.Liquid non-hydrocarbons refrigerant and steam non-hydrocarbons refrigerant can flow into the first flash drum 936 via pipeline 938.First
In flash drum 936, liquid non-hydrocarbons refrigerant can be separated with steam non-hydrocarbons refrigerant.
Steam non-hydrocarbons refrigerant from the first flash drum 936 can flow to pipe joint 930 via pipeline 940.Liquid is non-
Hydrocarbon refrigerant can be with flow ipe joint 942, and it can separate the liquid nonhydrocarbon that liquid non-hydrocarbons refrigerant is two separation
Class cold-producing medium stream.One liquid non-hydrocarbons cold-producing medium stream can flow through first heat exchanger 920, and partly or completely full flash distillation is steaming
Vapour, and return to pipe joint 930 via pipeline 928.Another liquid non-hydrocarbons cold-producing medium stream can flow via pipeline 946
To the second flash drum 944.Pipeline 946 can also include expansion valve 948, and it throttles liquid non-hydrocarbons cold-producing medium stream to control liquid
Non-hydrocarbons cold-producing medium stream flows into the second flash drum 944.Throttling of the liquid non-hydrocarbons cold-producing medium stream in expansion valve 948 can be led
Cause the flash distillation of liquid non-hydrocarbons cold-producing medium stream, the mixture of both generation steam and liquid non-hydrocarbons refrigerant.
Second flash drum 944 can separate steam non-hydrocarbons refrigerant with liquid non-hydrocarbons refrigerant.Steam non-hydrocarbons
Refrigerant can be via the flow ipe joint 950 of pipeline 952.Pipe joint 950 can with combined steam non-hydrocarbons refrigerant and from
Second and the 3rd steam non-hydrocarbons refrigerant reclaimed in heat exchanger 922 and 924.The steam non-hydrocarbons refrigerant of combination can be
Is compressed in compressor 954, and via the flow ipe joint 930 of pipeline 956, and from flash drum 936 and heat exchanger 920
Steam combination.
Liquid non-hydrocarbons refrigerant can flow to pipe joint 958 from the second flash drum 944, and it can separate liquid nonhydrocarbon
Class refrigerant is the liquid non-hydrocarbons cold-producing medium stream of two separation.One liquid non-hydrocarbons cold-producing medium stream flows through second heat exchanger
922 and return to pipe joint 950 via pipeline 960.Another liquid non-hydrocarbons cold-producing medium stream flows to the 3rd via pipeline 964
Flash drum 962.Pipeline 964 also includes expansion valve 966, and it controls liquid non-hydrocarbons cold-producing medium stream to flow into the 3rd flash drum 962.It is swollen
Swollen valve 966 may cause the flash distillation of liquid non-hydrocarbons cold-producing medium stream, the mixing of both generation steam and liquid non-hydrocarbons refrigerant
Thing.Flash distillation through valve will reduce the temperature and pressure of liquid non-hydrocarbons cold-producing medium stream.
The mixture of steam and liquid non-hydrocarbons refrigerant can be flashed into the 3rd flash drum 962, further reduction temperature
Degree and pressure.3rd flash drum 962 can separate steam non-hydrocarbons refrigerant with liquid non-hydrocarbons refrigerant.Steam non-hydrocarbons
Refrigerant can be via the flow ipe joint 968 of pipeline 970.Pipe joint 968 can with combined steam non-hydrocarbons refrigerant and from
The steam non-hydrocarbons refrigerant that third and fourth heat exchanger 924 and 926 is reclaimed.The steam non-hydrocarbons refrigerant of combination can be
Compressed and via the flow ipe joint 950 of pipeline 974 in compressor 972.
Liquid non-hydrocarbons refrigerant can be from the flow ipe joint 976 of the 3rd flash drum 962, and it can separate liquid nonhydrocarbon
Class refrigerant is the liquid non-hydrocarbons cold-producing medium stream of two separation.One liquid non-hydrocarbons cold-producing medium stream can flow through the 3rd heat friendship
Parallel operation 924 simultaneously returns to pipe joint 968 via pipeline 978.Another liquid non-hydrocarbons cold-producing medium stream can be via pipeline 980
Flow through the 4th heat exchanger 926.Pipeline 980 can also include expansion valve 982, and it allows liquid non-hydrocarbons refrigerant to flash, and
And therefore, as it flows into the pressure and temperature that the 4th heat exchanger 926 reduces liquid non-hydrocarbons cold-producing medium stream.From the 4th heat
Exchanger 926, liquid non-hydrocarbons cold-producing medium stream can be compressed in compressor 984 and be sent to pipe via pipeline 986
Road joint 968.
In one embodiment, including rare gas refrigerant mixture by flow through heat exchanger 920,922,
Each of 924 and 926 is pre-cooled.As discussed further below, refrigerant mixture can be via pipeline 988 from second
The heat exchanger 920,922,924 and 926 that refrigeration system 904 is flowed in the first refrigeration system 902.
After natural gas flow is progressively freezed in each of heat exchanger 920,922,924 and 926, it is via pipe
Line 990 flows into the second refrigeration system 904, as shown in Figure 9 B.Second refrigeration system 904 can include the He of the 5th heat exchanger 992
6th heat exchanger 994, it can be used for further cooled natural gas stream.5th heat exchanger 992 and the 6th heat exchanger 994 can
With using including the refrigerant mixture of one or more rare gas --- such as xenon or krypton --- come cooled natural gas stream.
Refrigerant mixture can be continuously circulated through the second refrigeration system 904, and it is prepared for entering heat exchanger
992 and 994 refrigerant mixture of each.Refrigerant mixture can be as vapor refrigerant mixture via pipeline
996 leave the 5th heat exchanger 992.Vapor refrigerant mixture can be mixed with the extra steam refrigerant in pipe joint 998
Compound is combined.Then vapor refrigerant mixture can flow through compressor 1000, and it can increase vapor refrigerant mixture
Pressure, produces the vapor refrigerant mixture of overheat.Superheated vapor refrigerant mixture can flow through gas cooler 1002, its
Superheated steam refrigerant mixture can be cooled down, liquid refrigerant mixture is produced.In some cases, if vapor refrigerant
Mixture is less than room temperature, then vapor refrigerant mixture may be without flow through gas cooler 1002.It is as discussed above, liquid refrigerating
Then agent composition can flow through the heat exchanger 920,922,924 and 926 in the first refrigeration system 902 via pipeline 988.
Once refrigerant mixture has already passed through heat exchanger 920,922,924 and 926, refrigerant mixture can be via
The 4th flash drum 1004 that pipeline 1006 enters in the second refrigeration system 904.Pipeline 1006 can include expansion valve 1008, and it is controlled
Refrigerant mixture processed flows into the 4th flash drum 1004.Expansion valve 1008 can reduce the temperature and pressure of refrigerant mixture
Power, causes refrigerant mixture to flash to both vapor refrigerant mixture and liquid refrigerant mixture.
Vapor refrigerant mixture and liquid refrigerant mixture can be flashed into the 4th flash drum 1004, and it can be by
Vapor refrigerant mixture is separated with liquid refrigerant mixture.Vapor refrigerant mixture can be flowed into via pipeline 1010 and managed
Road joint 998.Liquid refrigerant mixture can flow to pipe joint 1012 from the 4th flash drum 1004, and it can separate liquid
Refrigerant mixture is the liquid refrigerant mixture stream of two separation.One liquid refrigerant mixture stream can flow through the 5th
Heat exchanger 992 simultaneously returns to pipe joint 998 via pipeline 996.Another liquid refrigerant mixture stream can be via pipe
Line 1014 flows through the 6th heat exchanger 994.Pipeline 1014 can also include expansion valve 1016, and it controls liquid refrigerant mixture
Stream flows into the 6th heat exchanger 994, for example, by flashing refrigerant mixture, reducing temperature, and form steam-refrigerated
Agent composition and liquid refrigerant mixture.From the 6th heat exchanger 994, the vapor refrigerant mixture of gained can be in compression
Compressed in machine 1018, and then flow ipe joint 998 is recycled.
Natural gas flow is by with including the refrigerant of one or more rare gas in heat exchanger 992 and 994
Mixture indirect heat exchange and it is cooled after, natural gas flow can be flowed into via pipeline 1020 from refrigeration system 1000, such as Figure 10
It is shown.It can include the various parts for liquefied natural gas from refrigeration system 1000, produce LNG.
Natural gas flow can be with flow ipe joint 1022, and it can combine natural gas flow and a part from pipeline 1020
Natural gas flow 916.Before natural gas is via the flow ipe joint 1022 of pipeline 1026, the initial cooling of natural gas can be in heat friendship
Carried out in parallel operation 1024.
Natural gas can flow into reboiler 1028 from pipe joint 1022, and it can reduce the temperature of natural gas.Cooling
Natural gas can be expanded in the hydraulic buckling turbine 1030, and then flows into NRU systems 1032 via pipeline 1034 with from day
Excessive nitrogen is removed in right gas.In multiple embodiments, the low-temperature fractionation tower that natural gas is flowed into NRU systems 1032
1036, such as NRU towers.In addition, heat can be transferred to low-temperature fractionation tower 1036 from reboiler 1028 via pipeline 1037.
Low-temperature fractionation tower 1036 can separate nitrogen with natural gas via cryogenic distillation method.Overhead stream can be via
The outflow low-temperature fractionation of pipeline 1038 tower 1036.Overhead stream can mainly include methane and low boiling or non-condensable gas, for example
Nitrogen and helium, it is separated with natural gas.Overhead stream can flow into overhead condenser 1040, and it can separate overhead stream
Interior any liquid, and return to low-temperature fractionation tower 1036 using it as backflow.This may cause to produce steam stream, main
The fuel stream including methane and mainly include another steam stream of low-boiling point gas.The fuel stream can flow through via pipeline 1042
Heat exchanger 1024.In heat exchanger 1024, the temperature of vapor fuel stream can be via the indirect heat exchange with natural gas flow 916
And increase, produce vapor fuel stream.Then vapor fuel stream can be compressed in compressor 1044, and be used as fuel 1046
Via the outflow cascade cooling system 900 of pipeline 1048.Liquid flow from overhead condenser 1040 can be returned to as backflow stream
Low-temperature fractionation tower 1036.
The tower base stream produced in low-temperature fractionation tower 1036 mainly includes the natural gas with trace nitrogen.Tower base stream
And the steam stream from overhead condenser 1040 can flow into the 5th flash drum 1049 via pipeline 1050 and 1052 respectively.Pipe
Line 1050 can also include expansion valve 1054, and it controls tower base stream to flow into the 5th flash drum 1049, it is allowed to from bottom of towe
The liquid flashes of a part for logistics, form the mixed phase flow for flowing into the 5th flash drum 1049.
In addition, some parts of tower base stream can flow through overhead condenser 1040 via pipeline 1055.Pipeline 1055
Expansion valve 1056 can be included, it controls tower base stream to flow into overhead condenser 1040.Tower base stream may be used as tower top
The refrigerant of condenser 1040.The steam for leaving overhead condenser 1040 of gained can return to the 5th flash distillation via pipeline 1052
Drum 1049.
5th flash drum 1049 can separate multi-phase flow mainly to include the steam stream and LNG stream of natural gas.Steam stream can
With via the flow ipe joint 1058 of pipeline 1060.Pipe joint 1058 can be with combined steam stream and from the 6th flash drum 1062 times
Another steam stream received.The steam stream of combination can be compressed in the compressor 1064, and flows into the via pipeline 1066.
Pipe joint 912 in one refrigeration system 902.
LNG stream can flow into the 6th flash drum 1062 via pipeline 1068.Pipeline 1068 can include expansion valve 1070, its
Control LNG stream to flow into the 6th flash drum 1062, it is allowed to the liquid flashes of the part from LNG stream, formed and flow into the 6th flash distillation
The mixing phase system of drum 1062.
6th flash drum 1062 can separate mixed phase flow for LNG and the steam stream including natural gas.Steam stream can be through
By the flow ipe joint 1072 of pipeline 1074.What pipe joint 1072 can be reclaimed with combined steam stream and from the 7th flash drum 1076
Another steam stream.The steam stream of combination can be compressed and flow ipe joint 1058 in compressor 1078.
Then LNG stream can flow into the 7th flash drum 1076 via pipeline 1080.Pipeline 1080 can include expansion valve
1082, it controls LNG stream to flow into the 7th flash drum 1076, it is allowed to the liquid flashes of the part from LNG.7th flash distillation
Drum 1076 can further reduce the temperature and pressure of LNG stream so that LNG stream close to equilibrium temperature and pressure, such as below with reference to
What Figure 11 was discussed.The steam stream of generation can be with flow ipe joint 1084, and it can be reclaimed with combined steam stream and from LNG tank 1086
Boil-off gas.The steam stream of combination can be compressed and flow ipe joint 1072 in compressor 1088.
LNG tank 1086 can store LNG stream and continue any time section.The boil-off gas produced in the LNG tank 1086 can be with
Via the flow ipe joint 1084 of pipeline 1090.Point at any time, LNG stream can use pump 1094 to be transported to LNG oil tanks
Car (tanker) 1092, for transporting to market.The extra boil-off gas produced when LNG stream is loaded into LNG oil trucks 1092
Body 1098 can be reclaimed by being added into pipe joint 1084 in cascade cooling system 900.
It should be understood that Fig. 9 A, 9B and 10 process chart are not intended to show cascade cooling system 900 and from refrigeration system
1000 all parts including being shown in Fig. 9 A, 9B and 10.Moreover, according to the details of specific implementation, cascading cooling system 900
And/or can include any amount of additional components not shown in Fig. 9 A, 9B and 10 from refrigeration system 1000.For example, one
In a little embodiments, cascade cooling system 900 is using the refrigerant of the single mixing including at least one rare gas
One or more refrigeration systems.However, cascading cooling system 900 and/or can also include any other from refrigeration system 1000
The combination of the refrigeration system or refrigeration system of type.
Figure 11 is pressure of methane-enthalpy (P-H) Figure 110 0 schematic diagram.P-H Figure 110 0 shows phase at various temperatures
The pressure 1102 and enthalpy 1104 answered.The entry of identical numbering is as described on Fig. 9.P-H Figure 110 0 includes the profile of equilibrium 1106.
The left side 1108 of the profile of equilibrium 1106 represents neat liquid, and the right side of the profile of equilibrium 1106 represents pure gas 1110.If in addition,
The pressure 1102 and enthalpy 1104 of methane are in the profile of equilibrium 1106, then methane exists as the equilibrium mixture of liquids and gases.
If the pressure 1102 and enthalpy 1104 of methane are in critical condition in the profile of equilibrium more than 1106, methane.
According to autorefrigerated process described herein, expect to reduce the temperature and pressure 1102 of methane so that methane is as close
The liquid of atmospheric pressure is present.Each flash distillation in expansion valve 1056,1070 and 1080 and flash drum 1049,1062 and 1076
Reduce the temperature and pressure of methane process constant enthalpy.For example, before the expansion through hydraulic buckling turbine 1030, methane can
With in critical condition 1112.In many cases, it is difficult to reach using typical hydrocarbon coolant such as methane such critical
State.Therefore, in some cases, xenon replaces methane to can be used for autorefrigerated process.
Hydraulic buckling turbine 1030 can reduce the equilibrium state of temperature and pressure 1102 to the first 1114 of methane with constant enthalpy.
NRU can be operated in the first equilibrium state 1114 or under the pressure of somewhat higher.First equilibrium state 1114 can include big liquid
Body portion 1116 and small gas part 1118.Gas can discharge the 5th flash drum 1049 so that methane is in the first pure liquid
1120.However, the first pure liquid 1120 may be at being significantly higher than under the pressure 1102 of atmospheric pressure.Therefore, methane can flow
Cross expansion valve 1070 and enter the 6th flash drum 1062.
Expansion valve 1070 can reduce the equilibrium state of temperature and pressure 1102 to the second 1122 of methane with constant enthalpy.Similar to
One equilibrium state 1118, the second equilibrium state 1122 can include big liquid portion and small gas part.Gas can discharge the 6th
Flash drum 1062 so that methane is in the second pure liquid 1124.However, the second pure liquid 1124 can be still within being significantly higher than
Under the pressure 1102 of atmospheric pressure.Therefore, methane can flow through expansion valve 1080 and enter the 7th flash drum 1076.
Expansion valve 1082 can reduce the temperature and pressure 1102 of methane to the 3rd equilibrium state 1126 with constant enthalpy.3rd balance
State 1126 can include big liquid portion and small gas part.Gas can discharge the 7th flash drum 1076 so that at methane
In the 3rd pure liquid 1128.In multiple embodiments, the pressure 1102 of the 3rd pure liquid 1128 can be close to atmospheric pressure.Cause
This, methane can be the form of final products, and can be exported as LNG.
LNG forming methods
Figure 12 is the process chart for forming LNG method 1200.In multiple embodiments, method 1200 can be with
Implement in the system 800,900 or 1000 in office what is described respectively above with respect to Fig. 8,9 or 10.
Method 1200 starts in square 1202, is frozen in refrigeration systems in this natural gas.Refrigeration system can be machine
Tool refrigeration system, valve expansion system, turbine expansion system or the like.Refrigeration system uses the refrigerant for including rare gas to mix
Compound.Rare gas can include xenon, krypton, argon or its any combination.In addition, refrigerant mixture can include nitrogen or hydrocarbon,
Such as methane, ethane, propane or butane.Used according to the refrigerant mixture of implementations described herein, including rare gas
In any amount of cooling stage with realize than hydrocarbon coolant provide deeper cooling.
In multiple embodiments, refrigerant mixture, to provide the refrigerant mixture of compression, and is compressed by compressing
Refrigerant mixture by being cooled with cooling fluid indirect heat exchange.The refrigerant mixture of compression can be inflated to cold
But the refrigerant mixture compressed, so as to produce expansion, cooling refrigerant mixture.Expansion, cooling refrigerant is mixed
Compound can go to heat exchange area, and it can include, such as cooler or evaporator.In addition, natural gas can by with it is outer
Portion's cooling fluid indirect heat exchange and compressed and cooled down.Natural gas and then the cooling that expansion can be used in heat exchange area
Refrigerant mixture freezed.
Natural gas can be freezed via one or more precooling steps using the first refrigerant mixture.First system
Refrigerant mixture can include rare gas, nitrogen or hydrocarbon, or its any combination.Natural gas can also be via one or more depths
Degree cooling step is freezed using second refrigerant mixture.Second refrigerant mixture can include rare gas, nitrogen
Or hydrocarbon, or its any combination.
At square 1204, natural gas from refrigeration system being liquefied to form LNG.In multiple embodiments, from
Refrigeration system includes being used to cool down the multiple expansion valves and flash drum with liquefied natural gas.Natural gas may pass through expansion valve flash distillation,
The pressure and temperature of natural gas is reduced, and produces vaporous fraction and liquid distillate.Vaporous fraction and liquid distillate can be by
Flash distillation enters flash drum, and it can separate vaporous fraction with liquid distillate.This process can in any amount of expansion valve and
Repeated in flash drum, until proper amount of natural gas has been converted into LNG.
It should be understood that Figure 12 process chart is not intended to perform in any particular order the step of showing method 1200,
Or all steps are included in each situation.Moreover, according to the details of specific implementation, any amount of extra step
It can be included in method 1200.For example, in refrigeration systems before cooled natural gas, natural gas can be in the first refrigeration system
In be cooled.In multiple embodiments, the first refrigeration system uses non-hydrocarbons refrigerant.
Although this technology may by a variety of changes and can preferred form of this influenceed, embodiments discussed above is only
Only show by way of example.However, again it should be understood that this technology is not intended to be limited to embodiment disclosed herein.'s
Really, this technology includes all replacements, change and the equivalent form of value fallen into the true spirit and scope of appended claims.
Claims (29)
1. the system for forming liquefied natural gas (LNG), including：
Refrigeration system, it configures to freeze natural gas using the refrigerant mixture for including xenon or krypton or its any combination；
First refrigeration system, its configure with before the natural gas flows into the refrigeration system using non-hydrocarbons refrigerant without
It is that the refrigerant mixture cools down the natural gas；With
From refrigeration system, its configure using use the natural gas of the freezing as itself-refrigerant is with by the natural of the freezing
Gas forms the LNG.
2. system according to claim 1, including it is described from the nitrogen rejection facility for freezing system upstream.
3. system according to claim 1 or 2, wherein the system configuration is to freeze the natural gas, for hydrocarbon dew point
Control.
4. system according to claim 1 or 2, wherein the system configuration is to freeze the natural gas, for natural gas
Liquid (NGL) is extracted.
5. system according to claim 1 or 2, wherein the system configuration is with by methane and lighter gas and carbon dioxide
Separated with heavier gas.
6. system according to claim 1 or 2, wherein the system configuration is used for liquefied petroleum gas (LPG) life to prepare
Produce the hydrocarbon of storage.
7. system according to claim 1 or 2, wherein the system configuration is with condensing reflux stream.
8. system according to claim 1 or 2, wherein the refrigerant mixture includes xenon, krypton, argon or nitrogen, or its
Any combination.
9. system according to claim 1 or 2, wherein the refrigeration system includes mechanical refrigeration system, valve expansion system
Or turbine expansion system, or its any combination.
10. system according to claim 1 or 2, wherein the refrigerant mixture includes hydrocarbon, and wherein described hydrocarbon bag
Include methane, ethane, propane or butane, or its any combination.
11. system according to claim 1 or 2, wherein the refrigeration system includes multiple cooling circulations.
12. system according to claim 1 or 2, wherein the refrigeration system includes multiple cooling circulations, it includes：
One or more precooling stages, wherein the refrigerant mixture includes rare gas, nitrogen or hydrocarbon, or its any group
Close, and
The cooling circulation of one or more depth, wherein the refrigerant mixture includes rare gas, nitrogen or hydrocarbon, or its is any
Combination.
13. system according to claim 1 or 2, wherein using including xenon or krypton in one or more cooling stages
The refrigerant mixture with realize than hydrocarbon coolant provide more depth cooling.
14. system according to claim 1 or 2, including nitrogen rejection facility, wherein using the bottom from the nitrogen rejection facility
Liquid charging stock to provide the reflux condenser being cooled at the top of the nitrogen rejection facility.
15. system according to claim 1 or 2, wherein the refrigerant mixture includes pure component refrigerants.
16. the method for forming liquefied natural gas (LNG), including：
Natural gas is freezed in refrigeration systems, wherein the refrigeration system, which is used, includes xenon or krypton or its refrigerant being combined
Mixture；
The natural gas is cooled down before the natural gas is freezed in the refrigeration system in the first refrigeration system, wherein described
First refrigeration system uses non-hydrocarbons refrigerant rather than the refrigerant mixture；With
In the natural gas for the freezing of being liquefied from refrigeration system to form the LNG.
17. method according to claim 16, wherein the natural gas is freezed in the refrigeration system to be included：
The refrigerant mixture is compressed to provide the refrigerant mixture of compression；
Optionally, the refrigerant mixture with the cooling fluid indirect heat exchange cooling compression is passed through；
The refrigerant mixture of the compression is expanded to cool down the refrigerant mixture of the compression, thus produce expansion, it is cold
But refrigerant mixture；
Refrigerant mixture that make the expansion, cooling goes to the first heat exchange area；
Optionally, the natural gas is compressed；
Optionally, by cooling down the natural gas with outside cooling fluid indirect heat exchange；With
Make the natural gas and the expansion, cooling refrigerant mixture heat exchange.
18. the method according to claim 16 or 17, wherein the refrigerant mixture includes nitrogen or hydrocarbon, or its is any
Combination.
19. the method according to claim 16 or 17, including via multiple expansion valves or hydraulic buckling turbine and flash drum
The natural gas is liquefied to form the LNG.
20. the method according to claim 16 or 17, including:
The natural gas is freezed using the first refrigerant mixture via one or more precooling steps, wherein first system
Refrigerant mixture includes rare gas, nitrogen or hydrocarbon, or its any combination, and
The natural gas is freezed using second refrigerant mixture via one or more depth cooling steps, wherein described second
Refrigerant mixture includes rare gas, nitrogen or hydrocarbon, or its any combination.
21. the method according to claim 16 or 17, being included in use in one or more cooling stages includes xenon or krypton
The refrigerant mixture with realize than hydrocarbon coolant provide more depth cooling.
22. the cascade cooling system for forming liquefied natural gas (LNG), including：
First refrigeration system, it is configured to cool down the natural gas using non-hydrocarbons refrigerant, wherein first refrigeration system
Including multiple first coolers, it configures to allow the indirect thermal between the natural gas and the non-hydrocarbons refrigerant to hand over
Change the cooling natural gas；
Second refrigeration system, it configures to freeze described cooling using the refrigerant mixture for including xenon or krypton or its any combination
Natural gas, wherein second refrigeration system includes multiple second coolers, its configure to allow via the natural gas and
Indirect heat exchange between the refrigerant mixture cools down the natural gas, wherein first refrigeration system is without using described
Refrigerant mixture cools down the natural gas；With
From refrigeration system, it is configured with from LNG described in the natural gas adsorption of the freezing, wherein the self cooling jelly system is including more
Individual expansion valve or hydraulic buckling turbine, or its any combination, and flash drum.
23. cascade cooling system according to claim 22, wherein first refrigeration system includes compressor and condensation
Device, compressor configuration is to compress the non-hydrocarbons refrigerant, and the condenser arrangement is to cool down the non-hydrocarbons refrigerant.
24. the cascade cooling system according to claim 22 or 23, wherein second refrigeration system include compressor and
Condenser, the compressor configuration is to compress the refrigerant mixture, and the condenser arrangement is mixed with cooling down the refrigerant
Compound.
25. the cascade cooling system according to claim 22 or 23, wherein the multiple first cooler includes evaporator,
It is configured with by least partly vaporizing the nonhydrocarbon via heat is transferred into the non-hydrocarbons refrigerant from the natural gas
Class refrigerant and cool down the natural gas.
26. the cascade cooling system according to claim 22 or 23, wherein the multiple second cooler includes evaporator,
It is configured with by being transferred to the refrigerant mixture vaporization refrigerant mixture from the natural gas via by heat
And freeze the natural gas of the cooling.
27. the cascade cooling system according to claim 22 or 23, wherein the LNG includes liquid distillate and residue vapor
Cut, and wherein described cascade cooling system includes liquid separation container, and it is configured with by the residue vapor cut and institute
State liquid distillate separation.
28. the cascade cooling system according to claim 22 or 23, including it is described from the nitrogen rejection facility for freezing system upstream.
29. the cascade cooling system according to claim 22 or 23, wherein the refrigerant mixture includes pure component system
Cryogen.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201261618290P | 2012-03-30 | 2012-03-30 | |
| US61/618,290 | 2012-03-30 | ||
| US201261695592P | 2012-08-31 | 2012-08-31 | |
| US61/695,592 | 2012-08-31 | ||
| PCT/US2013/028906 WO2013148075A1 (en) | 2012-03-30 | 2013-03-04 | Lng formation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104204698A CN104204698A (en) | 2014-12-10 |
| CN104204698B true CN104204698B (en) | 2017-09-08 |
Family
ID=49260995
Family Applications (1)
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| CN201380017937.3A Expired - Fee Related CN104204698B (en) | 2012-03-30 | 2013-03-04 | Liquefied natural gas is formed |
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| Country | Link |
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| US (1) | US20150013379A1 (en) |
| EP (1) | EP2831523A4 (en) |
| CN (1) | CN104204698B (en) |
| AP (1) | AP2014007963A0 (en) |
| AR (1) | AR090506A1 (en) |
| AU (1) | AU2013240459B2 (en) |
| CA (1) | CA2867436C (en) |
| CL (1) | CL2014002309A1 (en) |
| EA (1) | EA201491790A1 (en) |
| MX (1) | MX2014010572A (en) |
| MY (1) | MY166784A (en) |
| WO (1) | WO2013148075A1 (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2013356460B2 (en) * | 2012-12-04 | 2018-04-05 | Conocophillips Company | Use of low global-warming potential, low ozone depletion potential, low combustibility hydrofluoro-olefin, xenon or iodo compound refrigerants in LNG processing |
| SG11201504193VA (en) * | 2013-01-24 | 2015-08-28 | Exxonmobil Upstream Res Co | Liquefied natural gas production |
| CN104729233B (en) * | 2015-04-09 | 2017-03-22 | 上海理工大学 | Natural gas liquefaction system with combination of auto-cascade refrigeration system and pulse tube refrigerator |
| FR3039080B1 (en) * | 2015-07-23 | 2019-05-17 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD OF PURIFYING HYDROCARBON-RICH GAS |
| CA3193233A1 (en) * | 2016-06-13 | 2017-12-13 | Geoff Rowe | System, method and apparatus for the regeneration of nitrogen energy within a closed loop cryogenic system |
| EP3500809A1 (en) * | 2016-08-16 | 2019-06-26 | ExxonMobil Upstream Research Company | System and method for liquefying natural gas with turbine inlet cooling |
| CN106744633B (en) * | 2017-01-23 | 2019-02-01 | 山东宏达科技集团有限公司 | One kind is anti-to fire gas recovery system for oil |
| SG10201802888QA (en) * | 2018-01-24 | 2019-08-27 | Gas Tech Development Pte Ltd | Process and system for reliquefying boil-off gas (bog) |
| CN108441261B (en) * | 2018-05-09 | 2023-06-06 | 舒伟 | Nitrogen-containing methane-rich gas separation system and separation method based on argon circulation refrigeration |
| CA3101931C (en) * | 2018-06-07 | 2023-04-04 | Exxonmobil Upstream Research Company | Pretreatment and pre-cooling of natural gas by high pressure compression and expansion |
| WO2020214522A1 (en) * | 2019-04-15 | 2020-10-22 | Charles Matar | Subcooled cryogenic storage and transport of volatile gases |
| US11815308B2 (en) | 2019-09-19 | 2023-11-14 | ExxonMobil Technology and Engineering Company | Pretreatment and pre-cooling of natural gas by high pressure compression and expansion |
| JP7326483B2 (en) | 2019-09-19 | 2023-08-15 | エクソンモービル・テクノロジー・アンド・エンジニアリング・カンパニー | Pretreatment and precooling of natural gas by high pressure compression and expansion |
| CN114669164B (en) * | 2022-03-24 | 2023-03-28 | 浙江大学 | System and method for preparing high-purity helium from natural gas BOG |
| WO2024120656A1 (en) * | 2022-12-07 | 2024-06-13 | Nuovo Pignone Tecnologie - S.R.L. | Natural gas condensate processing |
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| US4411677A (en) * | 1982-05-10 | 1983-10-25 | Air Products And Chemicals, Inc. | Nitrogen rejection from natural gas |
| US6250105B1 (en) * | 1998-12-18 | 2001-06-26 | Exxonmobil Upstream Research Company | Dual multi-component refrigeration cycles for liquefaction of natural gas |
| CN101228405A (en) * | 2005-08-09 | 2008-07-23 | 埃克森美孚上游研究公司 | Natural gas liquefaction process for producing LNG |
| CN101392983A (en) * | 2008-11-10 | 2009-03-25 | 陈文煜 | Process for liquefying high methane gas |
| CN101400952A (en) * | 2006-02-07 | 2009-04-01 | 布鲁克斯自动化有限公司 | Methods of freezeout prevention for very low temperature mixed refrigerant systems |
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| DE2009401A1 (en) * | 1970-02-27 | 1971-09-09 | Linde Ag, 6200 Wiesbaden | Process for liquefying low-boiling gases |
| MY115506A (en) * | 1998-10-23 | 2003-06-30 | Exxon Production Research Co | Refrigeration process for liquefaction of natural gas. |
| US6532752B1 (en) * | 2002-03-28 | 2003-03-18 | Praxair Technology, Inc. | Food freezing system |
| JP2008503605A (en) * | 2004-06-18 | 2008-02-07 | エクソンモービル アップストリーム リサーチ カンパニー | Hydrocarbon fluid treatment plant design. |
| ES2582941T3 (en) * | 2004-11-15 | 2016-09-16 | Mayekawa Mfg. Co., Ltd. | Method and device for liquefaction and cryogenic refrigeration |
| US20070107464A1 (en) * | 2005-11-14 | 2007-05-17 | Ransbarger Weldon L | LNG system with high pressure pre-cooling cycle |
| US9528759B2 (en) * | 2008-05-08 | 2016-12-27 | Conocophillips Company | Enhanced nitrogen removal in an LNG facility |
-
2013
- 2013-03-04 US US14/378,073 patent/US20150013379A1/en not_active Abandoned
- 2013-03-04 CN CN201380017937.3A patent/CN104204698B/en not_active Expired - Fee Related
- 2013-03-04 WO PCT/US2013/028906 patent/WO2013148075A1/en active Application Filing
- 2013-03-04 AP AP2014007963A patent/AP2014007963A0/en unknown
- 2013-03-04 EP EP13769414.7A patent/EP2831523A4/en not_active Ceased
- 2013-03-04 EA EA201491790A patent/EA201491790A1/en unknown
- 2013-03-04 CA CA2867436A patent/CA2867436C/en not_active Expired - Fee Related
- 2013-03-04 MX MX2014010572A patent/MX2014010572A/en unknown
- 2013-03-04 AU AU2013240459A patent/AU2013240459B2/en active Active
- 2013-03-04 MY MYPI2014002447A patent/MY166784A/en unknown
- 2013-03-26 AR ARP130100985A patent/AR090506A1/en not_active Application Discontinuation
-
2014
- 2014-08-29 CL CL2014002309A patent/CL2014002309A1/en unknown
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4411677A (en) * | 1982-05-10 | 1983-10-25 | Air Products And Chemicals, Inc. | Nitrogen rejection from natural gas |
| US6250105B1 (en) * | 1998-12-18 | 2001-06-26 | Exxonmobil Upstream Research Company | Dual multi-component refrigeration cycles for liquefaction of natural gas |
| CN101228405A (en) * | 2005-08-09 | 2008-07-23 | 埃克森美孚上游研究公司 | Natural gas liquefaction process for producing LNG |
| CN101400952A (en) * | 2006-02-07 | 2009-04-01 | 布鲁克斯自动化有限公司 | Methods of freezeout prevention for very low temperature mixed refrigerant systems |
| CN101392983A (en) * | 2008-11-10 | 2009-03-25 | 陈文煜 | Process for liquefying high methane gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104204698A (en) | 2014-12-10 |
| CA2867436C (en) | 2019-04-09 |
| AR090506A1 (en) | 2014-11-19 |
| CA2867436A1 (en) | 2013-10-03 |
| EP2831523A4 (en) | 2016-08-10 |
| MY166784A (en) | 2018-07-23 |
| WO2013148075A1 (en) | 2013-10-03 |
| AU2013240459B2 (en) | 2016-01-14 |
| EA201491790A1 (en) | 2015-01-30 |
| AU2013240459A1 (en) | 2014-10-09 |
| US20150013379A1 (en) | 2015-01-15 |
| AP2014007963A0 (en) | 2014-09-30 |
| EP2831523A1 (en) | 2015-02-04 |
| CL2014002309A1 (en) | 2015-04-06 |
| MX2014010572A (en) | 2014-12-08 |
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