CN104204698A - Lng formation - Google Patents
Lng formation Download PDFInfo
- Publication number
- CN104204698A CN104204698A CN201380017937.3A CN201380017937A CN104204698A CN 104204698 A CN104204698 A CN 104204698A CN 201380017937 A CN201380017937 A CN 201380017937A CN 104204698 A CN104204698 A CN 104204698A
- Authority
- CN
- China
- Prior art keywords
- natural gas
- refrigerant mixture
- refrigeration system
- cooling
- gas
- 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.)
- Granted
Links
- 230000015572 biosynthetic process Effects 0.000 title abstract description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 526
- 239000003507 refrigerant Substances 0.000 claims abstract description 253
- 239000003345 natural gas Substances 0.000 claims abstract description 225
- 239000000203 mixture Substances 0.000 claims abstract description 205
- 238000005057 refrigeration Methods 0.000 claims abstract description 183
- 238000000034 method Methods 0.000 claims abstract description 109
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 89
- 229930195733 hydrocarbon Natural products 0.000 claims description 165
- 150000002430 hydrocarbons Chemical class 0.000 claims description 165
- 239000007788 liquid Substances 0.000 claims description 135
- 239000007789 gas Substances 0.000 claims description 132
- 238000001816 cooling Methods 0.000 claims description 130
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 85
- 239000004215 Carbon black (E152) Substances 0.000 claims description 82
- 229910052757 nitrogen Inorganic materials 0.000 claims description 42
- 238000007710 freezing Methods 0.000 claims description 41
- 230000008014 freezing Effects 0.000 claims description 41
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 28
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 22
- 230000006835 compression Effects 0.000 claims description 20
- 238000007906 compression Methods 0.000 claims description 20
- 239000002826 coolant Substances 0.000 claims description 16
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 14
- 239000001569 carbon dioxide Substances 0.000 claims description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 14
- 238000004519 manufacturing process 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
- 229910052743 krypton Inorganic materials 0.000 claims description 12
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 claims description 12
- 239000001294 propane Substances 0.000 claims description 11
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 10
- 239000003915 liquefied petroleum gas Substances 0.000 claims description 8
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 8
- 229910052786 argon Inorganic materials 0.000 claims description 7
- 239000001273 butane Substances 0.000 claims description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 6
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 239000012809 cooling fluid Substances 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 2
- 229910001873 dinitrogen Inorganic materials 0.000 claims 1
- 229910052756 noble gas Inorganic materials 0.000 abstract description 2
- 230000008569 process Effects 0.000 description 54
- 239000003502 gasoline Substances 0.000 description 27
- 230000004087 circulation Effects 0.000 description 22
- 238000007701 flash-distillation Methods 0.000 description 19
- 238000002156 mixing Methods 0.000 description 17
- 238000012545 processing Methods 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 15
- 238000003860 storage Methods 0.000 description 13
- 238000009833 condensation Methods 0.000 description 10
- 239000000446 fuel Substances 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 229920006395 saturated elastomer Polymers 0.000 description 10
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 8
- 230000005494 condensation Effects 0.000 description 8
- 239000011555 saturated liquid Substances 0.000 description 8
- 239000002253 acid Substances 0.000 description 7
- 238000001704 evaporation Methods 0.000 description 7
- 238000005194 fractionation Methods 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 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
- 239000000126 substance Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 229910001868 water Inorganic materials 0.000 description 6
- 230000001276 controlling effect Effects 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 239000000284 extract Substances 0.000 description 5
- 239000001307 helium Substances 0.000 description 5
- 229910052734 helium Inorganic materials 0.000 description 5
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 5
- 239000012071 phase 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
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 238000013459 approach Methods 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 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
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- RWRIWBAIICGTTQ-UHFFFAOYSA-N difluoromethane Chemical compound FCF RWRIWBAIICGTTQ-UHFFFAOYSA-N 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 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
- 239000003921 oil Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 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
- 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
- 238000004821 distillation Methods 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 238000000605 extraction Methods 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
- 229910052704 radon Inorganic materials 0.000 description 2
- SYUHGPGVQRZVTB-UHFFFAOYSA-N radon atom Chemical compound [Rn] SYUHGPGVQRZVTB-UHFFFAOYSA-N 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
- 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
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 150000001412 amines 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
- 230000008901 benefit 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
- 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
- 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
- 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
- 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
- 238000009434 installation Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 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
- 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
- 230000005855 radiation Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 239000013589 supplement 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
- 238000010257 thawing Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—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
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0087—Propane; Propylene
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/0097—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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- 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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Abstract
Systems and a method for the formation of a liquefied natural gas (LNG) are disclosed herein. The system includes a refrigeration system configured to chill a natural gas using a refrigerant mixture including a noble gas. The system also includes an autorefrigeration system configured to use the natural g self-refrigerant to form the LNG from the natural gas.
Description
The cross reference of related application
It is that liquefied natural gas forms the U.S. Provisional Patent Application number 61/695 of (LNG FORMATION) that the application requires title that on August 31st, 2012 submits to, the title that on March 30th, 592 and 2012 submits to is application (the USE OF NOBLE GASES IN LOW TEMPERATURE HYDROCARBON PROCESSING SYSTEMS of rare gas in low temperature hydrocarbon treatment system, apparatus and method, APPARATUS, AND METHODS) U.S. Provisional Patent Application number 61/618,290 rights and interests, are all incorporated to herein by reference with it.
Technical field
This technology relate generally to hydrocarbon reclaims and processing procedure field, and relates more specifically to form via process of refrigerastion the system and method for liquefied natural gas.Particularly, provide use to comprise that the cold-producing medium of one or more rare gas is formed the system and method for LNG by natural gas.
Background technology
This part intention is introduced the various aspects of this area, and it may be relevant to the illustrative embodiments of this technology.Believe that this discussion has helped to provide promotion to understand better the framework of the concrete aspect of this technology.Therefore, be to be understood that this part should read from this angle, and needn't admitting as prior art.
Many cryogenic refrigerating systems dependences for natural gas processing and liquefaction are used the cold-producing medium that comprises hydrocarbon component and nitrogen so that external refrigeration to be provided.This hydrocarbon component can comprise methane, ethane, ethene, propane and analog.Yet, because may need large heat transfer area so that the suitable refrigeration of natural gas to be provided, use and comprise that the cold-producing medium of hydrocarbon component and nitrogen may not be very effective.In addition, the combustibility of the hydrocarbon component in cold-producing medium may increase the danger relevant to process of refrigerastion.
Cryogenic refrigerating system for natural gas processing and liquefaction is often used synthetic cold-producing medium---for example R-404A or R-410A---as the substituting of cold-producing medium that comprises hydrocarbon component and nitrogen.Yet this synthetic cold-producing medium is only suitable for the level of refrigeration higher than about-100 °F.In some cases, lower level of refrigeration may be expected.
The people's such as Flynn International Patent Application Publication WO/2005/072404 has described a kind of cooling system, it comprises the first refrigerant circulation and second refrigerant circulation, described the first refrigerant circulation comprises the first cold-producing medium, and described second refrigerant circulation is included as the second refrigerant of low temperature component mixture.The disclosure also relates to a kind of cooling system, and it comprises the first refrigerant circulation and second refrigerant circulation, and described the first refrigerant circulation comprises the first cold-producing medium, and described second refrigerant circulation is included as the second refrigerant of non-reactive component.Second refrigerant is not containing fluorocarbon, Chlorofluorocarbons and hydrocarbon.At least a portion of second refrigerant condensation in second refrigerant circulation.Yet the disclosure does not relate to the cooling system from freeze cycle that comprises any type.
Relevant information is found in U.S. Patent number 4,533, and 372,4,923,493,5,265,428,5,062,270,5,120,338,6,053,007 and 5,956,971; U.S. Patent Application Publication No. 2002/0088249,2003/0177785,2007/0193303,2007/0227185,2008/0034789,2008/0087041,2009/0217701,2009/0266107,2010/0018248,2010/0107684,2010/0186445,2012/0031144,2012/0079852 and 2012/0125043; And International Patent Publication No. WO/2012/015554.Other potentially relevant information be found in International Patent Publication No. WO 2007/021351; Foglietta, J.H. wait people, " 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; U.S. Patent number 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.
Summary of the invention
Embodiment provides the system that is used to form liquefied natural gas (LNG).This system comprises refrigeration system, and it is configured to use the freezing natural gas of refrigerant mixture that comprises rare gas.This system also comprises from refrigeration system, its be configured to use natural gas as self-cold-producing medium to be to form LNG from natural gas.
Another embodiment provides the method that is used to form LNG.The method is included in freezing natural gas in refrigeration system, and wherein refrigeration system is used the refrigerant mixture that comprises rare gas.The method is also included within refrigeration system liquefied natural gas to form LNG.
Another embodiment provides the cascade cooling system that is used to form LNG.Cascade cooling system comprises the first refrigeration system, it is configured to use non-hydrocarbons refrigerant cools natural gas, wherein the first refrigeration system comprises a plurality of the first coolers, and it is configured to allow cooled natural gas via the indirect heat exchange between natural gas and non-hydrocarbons cold-producing medium.Cascade cooling system also comprises the second refrigeration system, it is configured to use the freezing natural gas of refrigerant mixture that comprises rare gas, wherein the second refrigeration system comprises a plurality of the second coolers, and it is configured to allow cooled natural gas via the indirect heat exchange between natural gas and refrigerant mixture.Cascade cooling system further comprises from refrigeration system, and it is configured to form LNG from natural gas, wherein from refrigeration system, comprises a plurality of expansion valves or hydraulic buckling turbine or its any combination and flash drum.
embodiment
Embodiments of the present invention can be included in any combination of the method and system shown in the paragraph of numbering below.This be not considered to likely the complete of embodiment enumerate because any amount of variation can be expected from the above description.
1. the system that is used to form liquefied natural gas (LNG), comprising:
Refrigeration system, it is configured to use the freezing natural gas of refrigerant mixture that comprises rare gas; With
From refrigeration system, its be configured to use natural gas as self-cold-producing medium to be to form LNG by natural gas.
2. according to the system described in paragraph 1, comprise the first refrigeration system, it is configured to use non-hydrocarbons refrigerant cools natural gas before natural gas flows into refrigeration system.
3. according to the system described in any one of paragraph 1 or 2, comprise the nitrogen rejection facility from refrigeration system upstream.
4. according to the system described in any one of paragraph 1-3, wherein said system configuration, with freezing natural gas, is controlled for hydrocarbon dew point.
5. according to the system described in any one of paragraph 1-4, wherein said system configuration, with freezing natural gas, is extracted for natural gas liquids (NGL).
6. according to the system described in any one of paragraph 1-5, wherein said system configuration with by methane with separated with heavier gas with carbon dioxide compared with lighter-than-air gas.
7. according to the system described in any one of paragraph 1-6, wherein said system configuration is with the hydrocarbon for the preparation of liquefied petroleum gas (LPG) production inventory.
8. according to the system described in any one of paragraph 1-7, wherein said system configuration flows with condensing reflux.
9. according to the system described in any one of paragraph 1-8, wherein refrigerant mixture comprises xenon or krypton, or its any combination.
10. according to the system described in any one of paragraph 1-9, wherein refrigerant mixture comprises xenon, krypton, argon or nitrogen, or its any combination.
11. according to the system described in any one of paragraph 1-10, and wherein refrigeration system comprises mechanical refrigeration system, valve expansion system or turbine expansion system, or its any combination.
12. according to the system described in any one of paragraph 1-11, and wherein refrigerant mixture comprises hydrocarbon, and wherein hydrocarbon comprises methane, ethane, propane or butane, or its any combination.
13. according to the system described in any one of paragraph 1-12, and wherein refrigeration system comprises a plurality of cool cycles.
14. according to the system described in any one of paragraph 1-13, and wherein refrigeration system comprises a plurality of cool cycles, and it comprises:
In one or more pre-cooled stages, wherein refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination, and
One or more degree of depth cool cycles, wherein refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination.
15. according to the system described in any one of paragraph 1-14, wherein in one or more cooling stages, utilizes the refrigerant mixture comprise rare gas so that the cooling of the more degree of depth that provides than hydrocarbon coolant to be provided.
16. according to the system described in any one of paragraph 1-15, comprises nitrogen rejection facility, wherein uses liquid charging stock from the bottom of nitrogen rejection facility so that the reflux condenser being cooled at the top of nitrogen rejection facility to be provided.
17. according to the system described in any one of paragraph 1-16, and wherein refrigerant mixture comprises pure component refrigerants.
18. are used to form the method for liquefied natural gas (LNG), comprising:
Freezing natural gas in refrigeration system, wherein refrigeration system is used the refrigerant mixture that comprises rare gas; With
At liquefied natural gas in refrigeration system to form LNG.
19. according to the method described in paragraph 18, is included in refrigeration system before freezing natural gas cooled natural gas in the first refrigeration system, and wherein the first refrigeration system is used non-hydrocarbons cold-producing medium.
20. according to the method described in any one of paragraph 18 or 19, and wherein in refrigeration system, freezing natural gas comprises:
Compression refrigeration agent composition is to provide the refrigerant mixture of compression;
Optionally, by the refrigerant mixture with cooling fluid indirect heat exchange cooled compressed;
The refrigerant mixture of inflate compression is with the refrigerant mixture of cooled compressed, thus generation refrigerant mixture that expand, cooling;
Make refrigerant mixture to the first heat exchange area described expansion, cooling;
Optionally, compressed natural gas;
Optionally, by with the cooling described natural gas of external refrigeration fluid indirect heat exchange; With
Make refrigerant mixture heat exchange natural gas and expansion, cooling.
21. according to the method described in any one of paragraph 18-21, and wherein rare gas comprises xenon or krypton.
22. according to the method described in any one of paragraph 18-21, and wherein refrigerant mixture comprises nitrogen or hydrocarbon, or its any combination.
23. according to the method described in any one of paragraph 18-22, comprises via a plurality of expansion valves or hydraulic buckling turbine and flash drum liquefied natural gas to form LNG.
24. according to the method described in any one of paragraph 18-23, comprising:
Via one or more pre-cooled steps, use the freezing natural gas of the first refrigerant mixture, wherein the first refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination, and
Via one or more degree of depth cooling steps, use the freezing natural gas of second refrigerant mixture, wherein second refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination.
25. according to the method described in any one of paragraph 18-24, is included in one or more cooling stages and uses the refrigerant mixture that comprises rare gas so that the cooling of the more degree of depth that provides than hydrocarbon coolant to be provided.
26. are used to form the cascade cooling system of liquefied natural gas (LNG), comprising:
The first refrigeration system, it is configured to use non-hydrocarbons refrigerant cools natural gas, and wherein the first refrigeration system comprises a plurality of the first coolers, and it is configured to allow via the indirect heat exchange cooled natural gas between natural gas and non-hydrocarbons cold-producing medium;
The second refrigeration system, it is configured to use the freezing natural gas of refrigerant mixture that comprises rare gas, wherein the second refrigeration system comprises a plurality of the second coolers, and it is configured to allow via the indirect heat exchange cooled natural gas between natural gas and refrigerant mixture; With
From refrigeration system, it is configured to form LNG from natural gas, wherein from refrigeration system, comprises a plurality of expansion valves or hydraulic buckling turbine, or its any combination, and flash drum.
27. according to the cascade cooling system described in paragraph 26, and wherein the first refrigeration system comprises compressor and condenser, and described compressor configuration is with compression non-hydrocarbons cold-producing medium, and described condenser arrangement is with cooling non-hydrocarbons cold-producing medium.
28. according to the cascade cooling system described in any one of paragraph 26 or 27, and wherein the second refrigeration system comprises compressor and condenser, and described compressor configuration is with compression refrigeration agent composition, and described condenser arrangement is with cooling refrigeration agent composition.
29. according to the cascade cooling system described in any one of paragraph 26-28, and wherein a plurality of the first coolers comprise evaporimeter, and it is configured to by via heat being transferred to from natural gas to non-hydrocarbons cold-producing medium vaporize at least partly non-hydrocarbons cold-producing medium and cooled natural gas.
30. according to the cascade cooling system described in any one of paragraph 26-29, and wherein a plurality of the second coolers comprise evaporimeter, and it is configured to by the freezing natural gas via heat being transferred to from natural gas to refrigerant mixture gasified refrigerant mixture.
31. according to the cascade cooling system described in any one of paragraph 26-30, and wherein LNG comprises liquid distillate and residue vapor cut, and its cascade cooling system comprises fluid separation applications container, and it is configured to residue vapor cut separated with liquid distillate.
32. according to the cascade cooling system described in any one of paragraph 26-31, comprises the nitrogen rejection facility from refrigeration system upstream.
33. according to the cascade cooling system described in any one of paragraph 26-32, and wherein refrigerant mixture comprises pure component refrigerants.
Although this technology may be subject to the impact of multiple change and optional form, embodiment discussed above only illustrates in the mode of example.Yet, be again to be understood that this technology is not intended to be limited to the specific embodiment disclosed herein.Really, this technology comprises and falls into the true spirit of claims and all replacements, change and the equivalent form of value in scope.
accompanying drawing summary
By reference to following the detailed description and the accompanying drawings, understand better the advantage of this technology, wherein:
Fig. 1 is the process chart of single-stage refrigerating system;
Fig. 2 is the process chart that comprises the Two-stage refrigerating system of gasoline economizer;
Fig. 3 is the process chart that comprises the single-stage refrigerating system of heat exchanger gasoline economizer;
Fig. 4 is the process chart that comprises the cascade cooling system of the first refrigeration system and the second refrigeration system;
Fig. 5 is the process chart for the expansion refrigeration system of hydrocarbon dew point control;
Fig. 6 is the process chart for the expansion refrigeration system of NGL extraction;
Fig. 7 is the process chart of LNG production system;
Fig. 8 is the process chart of the simplification of cascade cooling system;
Fig. 9 A-B is the more detailed process chart of cascade 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 that is used to form the method for LNG.
accompanying drawing describes in detail
Following, describe in detail in part, described the specific embodiment of this technology.Yet, with regard to following description, be for the specific embodiment of this technology and the situation of concrete purposes, the description that it is only intended to exemplary purpose and illustrative embodiments is provided simply.Therefore, the specific embodiment that this technology is not limited to the following describes, but comprise all variations, modification and the equivalent form of value in the spirit and scope that fall into claims.
At first, for ease of reference, their meaning of having listed some term using in this application and having used in context.Situation about not limiting below with regard to term used herein, should provide its people in association area and provide the widest restriction of that term, as is embodied in the patent of at least one printed publication or distribution.And the use of the term that this technology can't help to illustrate below limits, because all equivalent form of values, synonym, new development and provide the term of same or similar object or technology to be considered in the scope of this claim.
" sour gas " is the pollutant often running in natural gas flow.Typically, although any amount of other pollutants also can form acid, these gases comprise carbon dioxide (CO
2) and hydrogen sulfide (H
2s).Sour gas is conventionally by by air-flow and absorbent---amine for example, and it can react with sour gas---and contact and remove.When absorbent becomes " being rich in " sour gas, can use desorption procedure with from absorbent separating acid gas.Then " poor " absorbent is typically recycled for further absorption." liquid acid gas stream " is the acid gas stream that is condensed into liquid phase as used herein, for example, comprises and is dissolved in H
2the CO of S
2and vice versa.
As used herein, " from freezing (certainly refrigeration, autorefrigeration) " refer to via the process that reduces pressure cooling fluid.The in the situation that of liquid, from freezing, refer to by evaporative cooling liquid, described evaporation is corresponding to reducing pressure.More specifically, while passing throttling arrangement along with it, withstanding pressure reduces, and the liquid of a part is flashed as steam.As a result, steam and residual liquid the two be all cooled to this liquid saturation temperature under reduced pressure.For example, according to embodiment described herein, natural gas from freezing can be by keeping the boiling point of natural gas in it to carry out along with heat loss natural gas is cooled during evaporating.The method also can be called as " flash distillation ".
As used herein, " cascade circulation " refers to the system with two or more cold-producing mediums, the first condensation of refrigerant that wherein cold second refrigerant is warmed up.Therefore, low temperature can by from a cold-producing medium downwards " cascade " to another.The stage evaporating pressure of every kind of cold-producing medium in cascade based in gasoline economizer can have a plurality of freezing levels.Because lower temperature in can obtaining than unitary system refrigerant system in cascade circulation, is considered to useful to producing LNG so cascade circulation is compared with unitary system refrigerant system.
" closed-loop refrigeration cycle " refers to and wherein there is no in the normal operation period that cold-producing medium enters or leave the kind of refrigeration cycle of circulation.
" closed-loop refrigeration system " refers to the refrigeration system that comprises compression, heat exchange and pressure regulating equipment, and wherein cold-producing medium recycles and do not have continuous deliberate cold-producing medium to regain.Due to the little leakage loss from system, typically need a small amount of cold-producing medium to supplement.
" compressor " or " coolant compressor " comprises any unit, equipment or the device of the pressure that can increase cold-producing medium stream.This comprises the coolant compressor with single compressed process or step, or has the coolant compressor of multi-stage compression or step, more specifically the multi-stage refrigerating agent compressor in single cover or shell.The cold-producing medium stream for the treatment of compressed evaporation can be provided to coolant compressor under different pressures.Some stages of hydrocarbon cooling procedure or step can comprise two or more parallel connections, series connection or both coolant compressors.The present invention can't help the type of one or more coolant compressors or arrangement or layout and limits, particularly in any refrigerant loop.
" controlled freeze district " (CFZ) method is the freezing potential that has been proposed to utilize the carbon dioxide in low temperature distillation, rather than avoids the method for solid carbon dioxide.In CFZ method, acid gas components is separated by low temperature distillation with thawing by the controlled freeze of the carbon dioxide in single tower, and does not use freezing suppressant additive.The low temperature distillation tower that CFZ method is used has special interior section---for example CFZ part---, to process solidifying and melting of carbon dioxide.This CFZ part does not comprise filler (packing) or tower tray (tray) as traditional destilling tower.But CFZ partly comprises one or more spray nozzles and thaw bowl.In the vapor space of solid carbon dioxide in destilling tower, form and drop on and on thaw bowl, become liquid.The all solid substantially forming is all limited in CFZ part.On the CFZ of tower part and under destilling tower be partly similar to traditional low temperature domethanizing column.The more detailed description of CFZ method is in U.S. Patent number 4,533,372; 4,923,493; Open in 5,120,338 and 5,265,428.
As used herein, temperature and/or interior for example any suitable amount of the reduction of " cooling " general reference and/or decline material.Coolingly can comprise that at least about 1 degree Celsius, at least about 5 degrees Celsius, at least about 10 degrees Celsius, at least about 15 degrees Celsius, at least about 25 degrees Celsius, at least about 50 degrees Celsius, the temperature of at least about 100 degrees Celsius and/or similar temperature reduce.Coolingly can use any suitable heat radiation, for example steam generation, hot water heating, cooling water, air, cold-producing medium, other process flow (comprehensively) and its combination.Can in conjunction with and/or the cooling one or more sources of cascade, to reach the outlet temperature of expectation.Cooling step can be used the cooling unit with any suitable device and/or equipment.According to an embodiment, coolingly can comprise indirect heat exchange, for example there are one or more heat exchangers.Heat exchanger can comprise any suitable design, for example surface of shell-and-tube, plate and framework, adverse current, following current, extension and/or analog.In substituting, the cooling cooling and/or direct heat of evaporation (heat of evaporation) of can using exchanges, for example, be directly injected to the liquid in process flow.
" low temperature " refers to approximately-50 ℃ or following temperature.
As used herein, term " dethanizer " and " domethanizing column " refer to distillation column or the tower for separating of the component in natural gas flow.For example, domethanizing column is for separated with heavier component with ethane with other volatile components by methane.Methane fraction is typically recovered as and comprises a small amount of inert gas for example nitrogen, CO
2or the purified gases of analog.
Term " gas " is used convertibly with " steam ", and is defined as in being different from material or the mixture of substances of liquid or solid-state gaseous state.Similarly, term " liquid " meaning is in being different from gaseous state or solid-state liquid material or mixture of substances.
" heat exchanger " looks like is widely heat can be delivered to any equipment of another medium from a medium, comprises especially any structure, for example, be commonly called the equipment of heat exchanger.Heat exchanger comprises " direct heat exchanger " and " indirect heat exchanger ".Therefore, heat exchanger can be plate-and-framework, shell-and-pipe, coil pipe, hairpin structure, core formula, core-and-the known heat exchanger of still (core-and-kettle), sleeve pipe or any other type." heat exchanger " also may refer to any post, tower, unit or other layouts, described layout is applicable to allowing one or more stream from wherein passing through, and affects one or more pipelines of cold-producing medium and the direct or indirect heat exchange between one or more feed stream.
" hydrocarbon " is the organic compound that mainly comprises element hydrogen and carbon, but nitrogen, sulphur, oxygen, metal or a plurality of other elements can be to exist in a small amount.As used herein, hydrocarbon generally refers to the component of finding in natural gas, oil or chemical process equipment.
" HFC " or HFC are the molecules that comprises H, F and C atom.HFC has H-C and F-C key and according to the C-C key of the number of the carbon atom in kind.Some examples of HFC comprise fluoroform (CHF
3), pentafluoroethane (C
2hF
5), HFC-134a (C
2h
2f
4), heptafluoro-propane (C
3hF
7), HFC-236fa (C
3h
2f
6), pentafluoropropane (C
3h
3f
5) and tetrafluoropropane (C
3h
4f
4), and the compound of other similar chemical constitutions.
" liquefied natural gas " or " LNG " is conventionally the known natural gas that comprises high percentage methane.Yet LNG also can comprise other compounds of trace.Other elements or compound can comprise, but be not limited to, ethane, propane, butane, carbon dioxide, nitrogen, helium, hydrogen sulfide or its combination, it is processed for example, (to remove one or more components, helium) or impurity (for example, water and/or heavy hydrocarbon) and be then almost condensed into liquid under atmospheric pressure by cooling.
The pre-cooled refrigerant system of mixing and the refrigerant system of two mixing of unitary system cooling system, hydrocarbon that the cold-producing medium that " the cold-producing medium method of mixing " can include, but not limited to use to mix---has the cold-producing medium more than a kind of chemical constituent---.Conventionally, the cold-producing medium of mixing can comprise hydrocarbon and/or non-hydrocarbon component.The example of the suitable hydrocarbon component typically adopting in the cold-producing medium mixing can include, but not limited to methane, ethane, ethene, propane, propylene and butane and butylene isomer.The non-hydrocarbon component usually adopting in the cold-producing medium mixing can comprise carbon dioxide and nitrogen.The cold-producing medium method of mixing adopts the cold-producing medium of at least one blending ingredients, but also can adopt extraly the cold-producing medium of one or more pure components.
" natural gas " refers to from crude oil well or the multicomponent gas that obtains from underground gas-bearing formation.The composition of natural gas and pressure can change significantly.Typical natural gas flow comprises methane (CH
4) as key component, that is, the natural gas flow that is greater than 50 % by mole is methane.Natural gas flow also can comprise ethane (C
2h
6), hydrocarbon with higher molecular weight (for example, C
3-C
20hydrocarbon), one or more sour gas (for example, carbon dioxide or hydrogen sulfide) or its any combination.Natural gas also can comprise a small amount of pollutant, for example water, nitrogen, iron sulfide, wax, crude oil or its any combination.Can be by purifying substantially, to remove the compound that can serve as poisonous substance before natural gas flow is used in embodiment.
As used herein, " natural gas liquids " (NGL) to refer to its component be the mixture of the hydrocarbon heavier than ethane typically for example.Some examples of the hydrocarbon component of NGL stream comprise propane, butane and pentane isomers, benzene, toluene and other aromatic compounds.
" rare gas " refers to any chemical element that belongs to 18 families of periodic table.More specifically, rare gas comprises helium (He), neon (Ne), argon (Ar), krypton (Kr), xenon (Xe) and radon (Rn).Rare gas is characterised in that to have low-down chemical reactivity.
" open loop refrigeration cycle " refers to kind of refrigeration cycle like this, and at least a portion of the cold-producing medium wherein adopting in the normal operation period is derived from the cooling fluid of kind of refrigeration cycle.
" open-loop refrigeration system " is the refrigeration system that comprises compression, heat exchange and decompressor, wherein cold-producing medium recirculation, and the cold-producing medium of a part is regained from recirculation circuit continuously, and extra cold-producing medium is introduced recirculation circuit continuously.
" refrigerant component " in refrigeration system will absorb heat by evaporation under lower temperature and pressure, and will under higher temperature and pressure, by condensation, discharge heat.Graphic refrigerant component can include, but not limited to have alkane, alkene and the alkynes of one to five carbon atom, nitrogen, chlorinated hydrocabon, fluorinated hydrocarbons, other halogenated hydrocarbons, rare gas and its mixture or composition.
When the quantity about material or its concrete property or amount are used, " substantially " refers to the amount that the effect that material or characteristic intention provide is enough provided.In some cases, the accurate extent of deviation of permission can be according to concrete context.
general introduction
Embodiment described herein provides hydrocarbon system of processing and method.Such hydrocarbon system of processing can comprise or utilize refrigeration system, for example cascade cooling system.And according to embodiment described herein, refrigeration system utilization comprises the refrigerant mixture of rare gas.
Hydrocarbon system of processing comprises legacy system well known by persons skilled in the art.Hydrocarbon is produced and processing method include, but not limited to freezing natural gas for NGL extract, freezing natural gas for hydrocarbon dew point control, freezing natural gas for CO
2remove, the condensation of the backflow in liquefied petroleum gas (LPG) production inventory, dethanizer/domethanizing column and natural gas liquefaction to be to produce LNG.
Although a plurality of kind of refrigeration cycle are for processing hydrocarbon, a circulation of using in LNG liquefying plant is cascade circulation, and it progressively uses a plurality of one-component cold-producing mediums in the heat exchanger of installation, with the temperature that reduces gas to condensing temperature.Another circulation of using in LNG liquefying plant is multiple group sub-refrigerating circulation, and it uses the multi-component refrigrant in specially designed interchanger.In addition, another circulation of using in LNG liquefying plant is expander circulation, and it is along with corresponding temperature reduces expansion gas from material pressure to low pressure.NG Liquefaction cycle also can be used variation or the combination of these three kinds of circulations.
LNG is prepared by unstripped gas by refrigeration and liquefaction technology.Optional step comprises that condensate removes, CO
2remove, dehydration, mercury remove, nitrogen stripping (stripping), H
2s removes etc.After liquefaction, LNG can be stored or be fed to gas pipeline for selling or using.Traditional liquifying method can comprise: APCI propane pre-cooling mix refrigerant but; C3MR; DUAL MR; The cascade of Phillips optimum; The cold-producing medium of the single mixing of Prico; The cold-producing medium that the two pressure of TEAL mixes; The cascade of Linde/Statoil multithread body; The two cold-producing mediums that mix of Axens, DMR; With Shell method C3MR and DMR.
Carbon dioxide removes, and is about to methane and compared with lighter-than-air gas and CO
2separated with heavier gas, can use K cryogenic treatment to realize, for example, from the obtainable controlled freeze of Exxon Mobil Corporation district technology.
Although about formed LNG by natural gas, method and system described herein has been discussed, the method and system also can be used for multiple other objects.For example, method and system described herein can be used for cooled natural gas and controls for hydrocarbon dew point, carrying out natural gas liquids (NGL) extracts, by methane with separated with heavier gas with carbon dioxide compared with lighter-than-air gas, prepare that hydrocarbon is produced for LPG or the backflow of condensation dethanizer and/or domethanizing column, etc.
cold-producing medium
According to the cold-producing medium of embodiment utilization described herein, can be one or more one-component cold-producing mediums, or comprise the refrigerant mixture of various ingredients.Cold-producing medium can comprise methane, ethane, ethene, propane, butane and nitrogen or its combination.In embodiment described herein, the cold-producing medium of one or more refrigeration in the stage used the nonflammable material that comprises rare gas and rare gas mixture.Cold-producing medium can be inputted or store by scene, or alternatively, some components of cold-producing medium can be typically by the still-process in situ preparation with the integration of hydrocarbon system of processing.The cold-producing medium of exemplary mixing is at U.S. Patent number 6,530, open in 240.
Comprise that the available cold-producing medium of business of fluorocarbon (FC) or HFC (HFC), for various application, comprises that ammonia, sulfur dioxide or halogenate hydrocarbon refrigerant are also like this.Exemplary refrigerant is available from DuPont Corporation business, comprises
cold-producing medium family,
cold-producing medium family,
cold-producing medium family and
cold-producing medium family.
Multi-component refrigrant is that business is available.For example, R-401A is the HCFC mixture of R-32, R-152a and R-124.R-404A is the HFC mixture of 52wt.%R-143a, 44wt.%R-125 and 4wt.%R-134a.R-406A is the mixture of 55wt.%R-22,4wt.%R-600a and 41wt.%R-142b.R-407A is the HFC mixture of 20wt.%R-32,40wt.%R-125 and 40wt.%R-134a.R-407C is the HFC mixture of R-32, R-125 and R-134a.R-408A is the HCFC mixture of R-22, R-125 and R-143a.R-409A is the HCFC mixture of R-22, R-124 and R-142b.R-410A is the mixture of R-32 and R-125.R-500 is the mixture of 73.8wt.%R-12 and 26.2wt.%R-152a.R-502 is the mixture of R-22 and R-115.
In embodiment described herein, the cold-producing medium in one or more refrigeration in the stage also can comprise rare gas or rare gas mixture.Six kinds of rare gas that naturally occur are helium (He), neon (Ne), argon (Ar), krypton (Kr), xenon (Xe) and radon (Rn).Rare gas can be used alone or is used in combination with other rare gas, or is used in combination with other refrigerant component.In some embodiments, the rare gas as cold-producing medium is xenon, krypton, argon or its combination.
Because rare gas is nonflammable, so they have reduced to process the danger of cold-producing medium.In addition, because rare gas is present in atmosphere, and easily collect, any rare gas cold-producing medium of effusion refrigeration system is recyclable.And if be discharged in environment, rare gas does not have any ozone and exhausts potential or greenhouse temperature increasing potential.
Rare gas cold-producing medium can provide lower than approximately-50 °F or lower than approximately-100 °F lower than approximately-120 °F or from approximately-50 °F to approximately-162 °F from approximately-50 °F to approximately-244 °F or from approximately-50 °F to about-303 °F cooling.In multistage refrigerating plant, can in the stage below, utilize rare gas cold-producing medium so that provide than hydrocarbon coolant darker cooling to be provided, for example, lower than approximately-50 °F, or lower than approximately-100 °F, or lower than approximately-120 °F, or from approximately-50 °F to approximately-162 °F, or from approximately-90 °F to approximately-162 °F, or from approximately-100 °F to approximately-162 °F, or from approximately-120 °F to approximately-162 °F, or from approximately-50 °F to approximately-244 °F, or from approximately-90 °F to approximately-244 °F, or from approximately-100 °F to approximately-244 °F, or from approximately-120 °F to approximately-244 °F, or from approximately-50 °F to approximately-303 °F, or from approximately-90 °F to approximately-303 °F, or from approximately-100 °F to approximately-303 °F, or from approximately-120 °F to approximately-303 °F.
In a plurality of embodiments, use together with any refrigeration system that any a plurality of dissimilar hydrocarbon systems of processing can be described with literary composition.In addition, refrigeration system described herein can be utilized any cold-producing medium described above.
refrigeration system
Hydrocarbon system and method generally include the refrigeration system of utilizing mechanical refrigeration, valve expansion, turbine expansion etc.Mechanical refrigeration typically comprises compressibility and absorption system, for example ammonia absorption system.Compressibility is used in gas processing industry, for a plurality of processes.For example, compressibility can be used for freezing natural gas for NGL extract, freezing natural gas for the condensation of the backflow of hydrocarbon dew point controls, LPG production inventory, dethanizer or domethanizing column, natural gas liquefaction with production LNG or similar application.And, utilize other commercialization process of refrigeration can utilize the intrinsic combustibility reducing of rare gas for example, to replace other cold-producing mediums, ammonia.
Fig. 1 is the process chart of single-stage refrigerating system 100.In a plurality of embodiments, single-stage refrigerating system 100 utilizes the refrigerant mixture that comprises rare gas.Single-stage refrigerating system 100 comprises expansion valve 102, cooler 104, compressor 106, condenser 108 and storage tank 110.Saturated liquid cold-producing medium 112 can flow to expansion valve 102 from storage tank 110, and can expand through expansion valve 102 on constant enthalpy ground (isenthalpically).During expansion, some appearance of vaporizing, form and to comprise the two freezing refrigerant mixture 114 of steam and liquid.Refrigerant mixture 114 can be than process flow 116---for example natural gas---to be cooled to the lower temperature of temperature under enter cooler 104, it is also referred to as evaporimeter.Process flow 116 flow through cooler 104 and with refrigerant mixture 114 exchanged heats.Along with process flow 116 and refrigerant mixture 114 exchanged heats, process flow 116 is cooled, and refrigerant mixture 114 can evaporate at least partly simultaneously, forms saturated vapor cold-producing medium 118.
Leave after cooler 104, saturated vapor cold-producing medium 118 and any remaining liquid refrigerant, interior compressed at compressor 106, and then flow into condenser 108.Within condenser 108, saturated vapor cold-producing medium 118 is converted into saturated or a little excessively cold liquid refrigerant 120.Then liquid refrigerant 120 can flow to storage tank 110 from condenser 108.Storage tank 110, is also referred to as surge tank or receiver, can serve as the reservoir (reservoir) of liquid refrigerant 120.Liquid refrigerant 120 can be stored in storage tank 110 as saturated liquid cold-producing medium 112 before expanding through expansion valve 102.
The process chart that is to be understood that Fig. 1 is not intended to show that single-stage refrigerating system 100 comprises all parts shown in Fig. 1.And according to the details of concrete enforcement, single-stage refrigerating system 100 can comprise unshowned any amount of extra parts in Fig. 1.For example, in some embodiments, refrigeration system can comprise two or more compression stages.In addition,, as further discussed about Fig. 2, refrigeration system 100 can comprise gasoline economizer.
Fig. 2 is the process chart that comprises the Two-stage refrigerating system 200 of gasoline economizer 202.The entry of identical numbering as described in Figure 1 on.Gasoline economizer 202 can be any equipment or the process reform that reduces the compressor horsepower utilization of the cooler work (duty) providing.Traditional gasoline economizer 202 comprises, for example, and flash tank and heat exchange gasoline economizer.
As shown in Figure 2, the saturated liquid cold-producing medium 112 that leaves storage tank 110 can expand can be separated to steam and liquid through expansion valve 102 intermediate pressure.Expansion valve 102 can be used for controlling downstream temperature and the pressure of saturated liquid cold-producing medium 112.For example, along with 112 flash distillations of saturated liquid cold-producing medium are through expansion valve 102, vapor refrigerant 204 and liquid refrigerant 206 produce under than the low pressure and temperature of saturated liquid cold-producing medium 112.Then vapor refrigerant 204 and liquid refrigerant 206 can flow into gasoline economizer 202.In a plurality of embodiments, gasoline economizer 202 is to realize vapor refrigerant 204 flash tank separated with liquid refrigerant 206.Vapor refrigerant 204 can flow to intermediate pressure compressor section, in this vapor refrigerant 204, can combine with the saturated vapor cold-producing medium 118 that leaves the first compressor 210, forms the saturated vapor cold-producing medium 208 mixing.Then the saturated vapor cold-producing medium 208 mixing can flow into the second compressor 212.
Liquid refrigerant 206 can from gasoline economizer 202 constant enthalpys expand through the second expansion valve 214.During expansion, some vaporizations can occur, form and comprise the two refrigerant mixture 216 of steam and liquid, reduce temperature and pressure.Refrigerant mixture 216 can have than the higher content liquid of refrigerant mixture not having in the system of gasoline economizer.Higher content liquid can reduce refrigerant circulation speed and/or reduce the power utilization of the first compressor 210.
Refrigerant mixture 216 than process flow 116 to be cooled to the lower temperature of temperature under enter cooler 104, it is also referred to as evaporimeter.As discussed above about Fig. 1, process flow 116 is cooled within cooler 104.In addition,, as discussed above about Fig. 1, saturated vapor cold-producing medium 118 flows through compressor 210 and 212 and condenser 108, and the liquid refrigerant 120 of gained is stored in storage tank 110.
The process chart that is to be understood that Fig. 2 is not intended to show that Two-stage refrigerating system 200 comprises all parts shown in Fig. 2.And according to the details of concrete enforcement, Two-stage refrigerating system 200 can comprise unshowned any amount of additional components in Fig. 2.For example, Two-stage refrigerating system 200 can comprise the equipment of unshowned other types in any amount of extra gasoline economizer or Fig. 2.In addition, gasoline economizer 202 can be heat exchange gasoline economizer rather than flash tank.Heat exchange gasoline economizer also can be for reducing kind of refrigeration cycle speed and reducing compressor horsepower utilization.
In some embodiments, Two-stage refrigerating system 200 comprises more than one gasoline economizer 202, and more than the compressor 210 and 212 of two.For example, Two-stage refrigerating system 200 can comprise two gasoline economizers and three compressors.Conventionally, if refrigeration system 200 comprises the gasoline economizer of X quantity, refrigeration system 200 will comprise the compressor of X+1 quantity.Such refrigeration system 200 with a plurality of gasoline economizers can form a part for cascade refrigeration system.
Fig. 3 is the process chart that comprises the single-stage refrigerating system 300 of heat exchanger gasoline economizer 302.The entry of identical numbering as described in Figure 1 on.As shown in Figure 3, the saturated liquid cold-producing medium 112 that leaves storage tank 110 can expand can separated intermediate pressure to steam and liquid through expansion valve 102, produces refrigerant mixture 114.Refrigerant mixture 114 can than process flow 116 to be cooled to the lower temperature of temperature under flow into cooler 104.As discussed above about Fig. 1, process flow 116 can be cooled in cooler 104.
Saturated vapor cold-producing medium 118 can flow through heat exchanger gasoline economizer 302 from cooler 104.Cold low-pressure saturated steam cold-producing medium 118 is used in heat exchanger gasoline economizer 302 and makes saturated liquid cold-producing medium 112 excessively cold.As discussed above about Fig. 1, then the superheated vapor refrigerant 304 of leaving heat exchanger gasoline economizer 302 can flow through compressor 106 and condenser 108, and the liquid refrigerant 120 of gained can be stored in storage tank 110.
The process chart that is to be understood that Fig. 3 is not intended to show that single-stage refrigerating system 300 comprises all parts shown in Fig. 3.And according to the details of concrete enforcement, single-stage refrigerating system 300 can comprise unshowned any amount of additional components in Fig. 3.
Fig. 4 is the process chart that comprises the cascade cooling system 400 of the first refrigeration system 402 and the second refrigeration system 404.In a plurality of embodiments, the utilization of the first refrigeration system 402 comprises for example cold-producing medium of xenon or krypton of rare gas, and the second refrigeration system 404 can be utilized different rare gas cold-producing medium, fluorocarbon refrigerants or hydrocarbon coolant.Refrigeration system 402 or 404 arbitrary in cold-producing medium can comprise mixture.The cooling situation of the higher degree that provides than refrigeration system 100,200 or 300 of expectation is provided cascade cooling system 400.Cascade cooling system 400 can provide cooling at for example lower than-40 ℃ in low-down temperature.
In the first refrigeration system 402, liquid refrigerant streams 406 can flow through the first expansion valve 410 and the first heat exchanger 412 from storage tank 408, its cooling products stream 413.The vapor/liquid stream of gained is separated in the first flash drum 414.The liquid refrigerant streams 406 of a part can flow directly into the first flash drum 414 via by-passing valve 416, and this can be used for controlling the temperature of the liquid in the first flash drum 414, and the cooling amount in the first heat exchanger 412.
Liquid refrigerant streams 418 can flow through the second expansion valve 420 from the first flash drum 414, and flash distillation enters the second heat exchanger 422, and it can be used for further cooling products stream 413.Vapor refrigerant stream 426 to the first stage compressor 428 of gas reservoir 424 supply gained.The intermediate pressure vapor refrigerant stream 430 of gained combines with the vapor refrigerant stream 432 from the first flash drum 414, and the stream of combination is supplied to second stage compressor 434.From the high steam stream 436 of second stage compressor 434, through condenser 438, it can use cooling from the second refrigeration system 404.Especially, condenser 438 can use the low-temperature refrigerant from the second refrigeration system 404 to flow 440 cooling high steam streams 436 to produce liquid refrigerant streams 406.Then liquid refrigerant streams 406 from condenser 438 is stored in storage tank 408.Control valve 442 can be used for controlling low-temperature refrigerant stream 440 and flows through condenser 438.The vapor refrigerant stream 444 of gained is got back to the second refrigeration system 404 from condenser 438.
In the second refrigeration system 404, liquid refrigerant streams 448 can flow through heat exchanger 452 from storage tank 450, and described heat exchanger 452 is configured to via refrigeration system 454 cooling liquid cold-producing medium streams 448.The low-temperature refrigerant stream 456 of gained can flow through the first expansion valve 458 and the first heat exchanger 460, its cooling products stream 413.The vapor/liquid cold-producing medium stream of gained is separated in the first flash drum 462.The low-temperature refrigerant stream 456 of a part can flow directly into the first flash drum 462 via by-passing valve 464, and this can be used for controlling the temperature of the liquid in the first flash drum 462, and the cooling amount in the first heat exchanger 460.
Liquid refrigerant streams 466 can flow through the second expansion valve 468 from the first flash drum 462, and flash distillation enters the second heat exchanger 470, and it can be used for further cooling products stream 413.The vapor/liquid cold-producing medium stream of gained is separated in the second flash drum 472.The liquid refrigerant streams 466 of a part can flow directly into the second flash drum 472 via by-passing valve 474, and this can be used for controlling the temperature of the liquid in the second flash drum 472, and the cooling amount in the second heat exchanger 470.
Liquid refrigerant streams 476 can flow through the 3rd expansion valve 478 from the second flash drum 472, and flash distillation enters the 3rd heat exchanger 480, and it can be used for further cooling products stream 413.Vapor refrigerant stream 484 to the first stage compressor 486 of gas reservoir 482 supply gained.The intermediate pressure vapor refrigerant stream 488 of gained combines with the vapor refrigerant stream 490 from the second flash drum 472, and the stream of combination is supplied to second stage compressor 492.The high steam cold-producing medium stream 494 of gained combines with the vapor refrigerant mixture 496 from the first flash drum 462, and the stream of combination is supplied to phase III compressor 497.The high steam cold-producing medium stream 498 of gained flows through heat exchanger 499, and described high steam cold-producing medium stream 498 is by being further cooled with cooling water indirect heat exchange therein.Then the liquid refrigerant streams 448 of gained can flow into storage tank 450.
The process chart that is to be understood that Fig. 4 is not intended to show that cascade cooling system 400 comprises all parts shown in Fig. 4.And according to the details of concrete enforcement, cascade cooling system 400 can comprise unshowned any amount of extra parts in Fig. 4.
Fig. 5 is the process chart for the expansion refrigeration system 500 of hydrocarbon dew point control.Heavy hydrocarbon in pipeline in natural gas is C for example
3-C
6condensation can cause manifold pressure to increase, and the power utilization for the treatment of facility increases.Therefore,, in order to prevent this condensation, can use expansion refrigeration system 500 to reduce hydrocarbon dew point.
As shown in Figure 5, the natural gas feedstream 502 of dehydration can inflow gas/gas heat-exchanger 504.In gas/gas heat exchangers 504, the natural gas feedstream 502 of dehydration can be cooled by flowing 506 indirect heat exchange with cryogenic natural gas.The natural gas flow 508 of gained can flow into the first separator 510, and it can shift out from natural gas flow 508 heavy hydrocarbon 512 of a tittle.In a plurality of embodiments, from natural gas flow 508, shift out the dew point that heavy hydrocarbon 512 has reduced natural gas flow 508.The heavy hydrocarbon 512 shifting out can flow out expansion refrigeration system 500 by the first outlet valve 514.For example, heavy hydrocarbon 512 can flow to stabilizer (not shown) from expansion refrigeration system 500.
Then natural gas flow 508 can flow into expander 516.In a plurality of embodiments, expander 516 is turbine expander, and it is radial outward flow turbine or axial turbine.The expansion of natural gas flow 508 in expander 516 can be provided for the energy of drive compression machine 518, and described 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 flow 506 from cryogenic natural gas and shift out any remaining heavy hydrocarbon 512.In a plurality of embodiments, from cryogenic natural gas stream 506, shift out the dew point that heavy hydrocarbon 512 has further reduced cryogenic natural gas stream 506.Then the heavy hydrocarbon 512 shifting out can flow out expansion refrigeration system 500 by the second outlet valve 524.
Cryogenic natural gas stream 506 can flow to gas/gas heat exchangers 504 from the second separator 522, and the temperature that it can increase cryogenic natural gas stream 506 produces high-temperature natural gas stream 526.Then high-temperature natural gas stream 526 can flow through compressor 518, and it can turn back to the pressure of natural gas flow 526 acceptable acid gas pressure.Finally, then the dew point natural gas flow 528 of reduction can flow out expansion refrigeration system 500.
In embodiment, for example, use the cooling system of rare gas cold-producing medium to can be used for to process increase further cooling.This cooling by cryogenic natural gas stream 506, the placed upstream heat exchanger 530 of the second separator 522 implements.Refrigerant liquid 532 can be by cooler 530 flash distillations by expansion valve 534.Then the refrigerant vapour 536 of gained can turn back to refrigerant system.The cooling condensable hydrocarbons that can allow to shift out much higher amount, for example C
3s and Geng Gao.And in some embodiments, heat exchanger 530 is placed on the upstream of expander 516, separator is between heat exchanger 530 and expander 516, to prevent that liquid from flowing into expander 516.
The process chart that is to be understood that Fig. 5 is not intended to show that expansion refrigeration system 500 comprises all parts shown in Fig. 5.And according to the details of concrete enforcement, expansion refrigeration system 500 can comprise unshowned any amount of additional components in Fig. 5.
Fig. 6 is the process chart for the expansion refrigeration system 600 of NGL extraction.In a plurality of embodiments, can implement NGL and extract to reclaim NGL, it comprises any amount of different heavy hydrocarbon from natural gas flow.Because NGL is often the fact of larger value, in order to be different from the object of gaseous state heating fuel, NGL extracts and can expect.
Dry natural gas feed stream 602 can be from dewatering system inflow gas/gas heat-exchanger 604.In gas/gas heat exchangers 604, can carry out cool drying natural gas feedstream 602 by flowing 606 indirect heat exchange with cryogenic natural gas.The natural gas flow 608 of gained can flow into separator 610, and it can shift out a part of NGL612 from natural gas flow 608.The NGL612 shifting out can flow into dethanizer or domethanizing column 614 from separator 610.
Then natural gas flow 608 can flow into expander 616.In a plurality of embodiments, expander 616 is turbine expander.The expansion of natural gas flow 608 in expander 616 can be provided for the energy of drive compression machine 618, and described compressor 618 is connected to expander 616 via axle 620.In addition, can through joule-Thomson valve 622, reduce via adiabatic expansion the temperature of natural gas flow 608.
The cryogenic natural gas stream 606 of gained can flow into dethanizer or domethanizing column 614 from expander 616.In dethanizer or domethanizing column 614, NGL can be separated with natural gas flow 606, and can be used as NGL product stream 624 outflow dethanizer or domethanizing columns 614.Then NGL product stream 624 can pump via pump 626 from expansion refrigeration system 600.
Dethanizer or domethanizing column 614 can be connected to heat exchanger 628.In some embodiments, heat exchanger 628 is reboilers 628, and it can be used for the tower base stream (bottoms stream) 630 from a part for dethanizer or domethanizing column 614 via the indirect heat exchange heating in high temperature fluid 632.Tower base stream 630 then can reinject dethanizer or the domethanizing column 614 of heating.
In dethanizer or domethanizing column 614, NGL product stream 624 and natural gas flow 606 separated may cause producing cryogenic natural gas stream, and it can be used as overhead stream (overhead stream) 634 and flows out dethanizer or domethanizing columns 614.Overhead stream 634 can inflow heat exchanger 636, and it can be by reducing the temperature of overhead streams 634 with comprising refrigerant mixture 638 indirect heat exchange of rare gas.The reduction of temperature can cause some steam-condensations.Overhead stream 634 then can be in the interior separation of separation container 640, to produce cryogenic natural gas stream 606 and liquid bottoms stream 642.Tower base stream 642 can be pumped back to dethanizer or domethanizing column 614 via pump 644, 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 can, in the interior rising of gas/gas heat exchangers 604, produce high-temperature natural gas stream 646.Then high-temperature natural gas stream 646 can flow through compressor 618, and it can increase the pressure of natural gas flow 646.In some embodiments, high-temperature natural gas stream 646 also flows through the second compressor 648, and its pressure that can increase natural gas flow 646 is to acceptable acid gas pressure.Then natural gas product stream 650 can flow out expansion refrigeration system 600.
The process chart that is to be understood that Fig. 6 is not intended to show that expansion refrigeration system 600 comprises all parts shown in Fig. 6.And according to the details of concrete enforcement, expansion refrigeration system 600 can comprise unshowned any amount of additional components in Fig. 6.
Fig. 7 is the process chart of LNG production system 700.As shown in Figure 7, use a plurality of different refrigeration systems, LNG702 can produce from natural gas flow 704.As shown in Figure 7, a part of natural gas flow 704 can be separated from natural gas flow 704 before entering LNG production system 700, and can be used as fuel gas stream 706.Remaining natural gas flow 704 can flow into initial gas processing system 708.In gas processing system 708, natural gas flow 704 can be purified with cooling.For example, can use rare gas cold-producing medium, for example, comprise the refrigerant mixture cooled natural gas stream 704 of one or more rare gas.For example, heavy hydrocarbon 710 can shift out from natural gas flow 706, and is used in the interior production gasoline 712 of heavy hydrocarbon system of processing 714.In addition, during producing gasoline 712, any remaining natural gas 716 separated with heavy hydrocarbon 710 can turn back to natural gas flow 704.
Natural gas flow 704 can be converted into LNG702 in low temperature heat exchanger 718.In some embodiments, from the cold-producing medium stream 720 of the mixing of the refrigeration system 722 of mixing at the interior cooled natural gas stream 704 of low temperature heat exchanger 718.According to embodiment described herein, the cold-producing medium of mixing stream 720 is the refrigerant mixtures that comprise one or more rare gas.In other embodiments, the hydrocarbon coolant stream (not shown) from hydrocarbon refrigeration system 724 is used at the interior cooled natural gas stream 704 of low temperature heat exchanger 718, to produce LNG702.
The process chart that is to be understood that Fig. 7 is not intended to show that LNG production system 700 comprises all parts shown in Fig. 7.And according to the details of concrete enforcement, LNG production system 700 can comprise unshowned any amount of additional components in Fig. 7.For example, any amount of optional refrigeration system also can be used for producing LNG702 from natural gas flow 704.In addition, any amount of different refrigeration system can be used in combination to produce LNG702.
cascade cooling system for the production of liquefied natural gas
Fig. 8 is the process chart of the simplification of cascade cooling system 800.Cascade cooling system 800 can be used for producing LNG802 from raw natural gas 804.Raw natural gas 804 can flow into the entrance washer 806 in cascade cooling system 800.Entrance washer 806 can remove unwanted particle from raw natural gas 804.Along with natural gas enters cascade cooling system 800, entrance gauge table 808 can be monitored amount and the characteristic of natural gas.Natural gas can pass through amine processor 810, and it can remove hydrogen sulfide, carbon dioxide and other unwanted gas from natural gas, and can be in 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 remove water 816 via gravity based separation process from natural gas.The water 816 removing can be from 800 outputs of cascade cooling system.Then natural gas can flow to the second dewaterer 818, and it can remove any remaining water from natural gas.The second dewaterer 818 for example can be, molecular sieve bed or zeolite beds.
Can comprise the mercury removal system 820 of molecular sieve bed can be from natural gas removal of mercury.In addition, dry gas filter 822, for example 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 a part heat exchanger and flash drum the two.Yet, in other are implemented, can use independent flash drum, the gasoline economizer 202 of for example discussing about Fig. 2.Therefore, the first ice chest 824 can be via carrying out cooled natural gas with the indirect heat exchange of the first refrigerant mixture 828.The first refrigerant mixture 828 can be traditional cold-producing medium, for example HFC or propane.In addition, the first ice chest 824 can serve as steam-liquid separator, and separated the first refrigerant mixture is vapor refrigerant mixture 830 and liquid refrigerant mixture.Vapor refrigerant mixture 830 can produce via the flash distillation of the first refrigerant mixture 828 through expansion valve 832.Expansion valve 832 can throttling the first refrigerant mixture 828 to reduce the pressure and temperature of the first refrigerant mixture 828, cause the flash distillation of the first refrigerant mixture 828.In some embodiments, the first refrigerant mixture 830 can be vaporized completely, and therefore, does not have liquid refrigerant mixture to may reside in the first ice chest 824.
The first refrigerant mixture 828 can recycle continuously and recycle in refrigeration system 826.For example, the first refrigerant mixture 828 is through after the first ice chest 824, and the vapor refrigerant mixture 830 of gained is can be interior compressed by the high pressure compressor 834 of the first gas turbine 836 energy supplies.High pressure compressor 834 can be by the energy supply of gas only turbine, for example, and by being placed on axle common or that connect, or can be by motor energy supply.Then vapor refrigerant mixture 830 is condensed into liquid refrigerant mixture 828 in the first condenser 838.Then liquid refrigerant mixture 828 can be stored in surge tank 840, and liquid refrigerant mixture can flow back into the first ice chest 824 to finish cool cycles from surge tank 840.
Second refrigerant mixture 842 is also used in the natural gas 823 of the second ice chest 844 interior further cooling purifying.In this example, the second ice chest 834 is via the natural gas 823 with comprising the next further cooling purifying of second refrigerant mixture 842 indirect heat exchange of at least one rare gas.In addition, the second ice chest 844 can serve as steam-liquid separator, and separated second refrigerant mixture 842 is vapor refrigerant mixture 846 and liquid refrigerant mixture.Vapor refrigerant mixture 846 can produce via the flash distillation of the second refrigerant mixture 842 through expansion valve 848.Expansion valve 848 can throttling second refrigerant mixture 842 to reduce the pressure and temperature of second refrigerant mixture 842, cause the flash distillation of second refrigerant mixture 842.In some embodiments, second refrigerant mixture 842 can be vaporized completely, and therefore, does not have liquid refrigerant mixture to may reside in the second ice chest 844.
The vapor refrigerant mixture 846 of leaving the gained of the second ice chest 844 can, interior compressed by the low pressure compressor 850 of the second gas turbine 852 energy supplies, produce the refrigerant mixture 85 of compression.Low pressure compressor 850 can be by the energy supply of gas only turbine, for example, and by being placed on axle common or that connect, or can be by motor energy supply.For example, in the refrigerant mixture 854 of compression then can be at low-temperature condenser 856---ammonia cooler---, be condensed to produce second refrigerant mixture 842.Second refrigerant mixture 842 can be stored in surge tank 858, and second refrigerant mixture 842 can flow back into the second ice chest 844 to finish cool cycles from surge tank 858.
After natural gas 823 is cooling in ice chest 824 and 844, natural gas 823 can be further cooled and liquefy in refrigeration system 860, produces LNG802.In some embodiments, from refrigeration system 860, comprise a series of expansion valve (not shown) and flash drum (not shown), it little by little reduces the temperature and pressure of natural gas, until natural gas under atmospheric pressure or approach atmospheric pressure and reach liquid.In addition, flowing into before refrigeration system 860, natural gas 823 can flow through high pressure nitrogen rejection facility (NRU) (not shown).NRU can remove the nitrogen of some parts from natural gas 823, and therefore, can allow to use the gas that contains high percentage nitrogen.
From refrigeration system 860, also can produce natural gas steam, it can be used as fuel 862.Fuel 862 can be interior compressed by the compressor 864 of the 3rd gas turbine 866 energy supplies before flowing out cascade cooling system 800.According to the demand to fuel 862, most natural gas steam can reconfigure with the natural gas 823 of initial purifying, and turns back in system for further processing.
The LNG802 producing can be stored in LNG tank 868 before being sent out cascade cooling system 800.Gas can be discharged out and be pumped back to from refrigeration system 860 via the first pump 870 from LNG tank 868.In addition, on charging appliance, load the gas 872 separated with LNG802 during LNG802, for example, can be pumped back into from refrigeration system 860 via the second pump 874.
The process chart that is to be understood that Fig. 8 is not intended to show that cascade cooling system 800 comprises all parts shown in Fig. 8.And according to the details of concrete enforcement, cascade cooling system 800 can comprise unshowned any amount of additional components in Fig. 8.
Fig. 9 A-C is the more detailed process chart of cascade cooling system 900.Cascade cooling system 900 can be for the production of the cascade of LNG, open loop liquefaction system.Cascade cooling system 900 can be at low temperature---for example, lower than about 0 °F or lower than approximately-20 °F or lower than approximately-40 °F---lower operation.In addition, cascade cooling system 900 can adopt more than a kind of cold-producing medium and at a plurality of temperature refrigeration is provided.
As shown in Figure 9 A, cascade cooling system 900 can comprise the first refrigeration system 902, and it can utilize for example HFC of non-hydrocarbons cold-producing medium, for example, and R-404A or R-410a.The refrigerant mixture that as shown in Figure 9 B, cascade cooling system 900 also can comprise the second refrigeration system 904, and it can utilize and comprise at least one rare gas---for example xenon, krypton, argon or its combination---.
Figure 10 is the more detailed process chart from refrigeration system 1000.As discussed further below, from refrigeration system 1000, can be positioned at the downstream of cascade cooling system 900.
Natural gas flow 908 can flow into the pipe joint 910 in cascade cooling system 900.It is two separated natural gas flows that pipe joint 910 can be configured to separately natural gas flow 908.A natural gas flow 914 can flow into another pipe joint 912, and another natural gas flow 916 can flow into from refrigeration system 1000.
In pipe joint 912, natural gas flow 914 can combine with the natural gas vapor stream 1066 from from refrigeration system 1000.Then the natural gas flow 918 of gained can flow into the first refrigeration system 902, prepares for cooled natural gas stream 918.Natural gas flow 918 can be cooled by a series of heat exchangers 920,922,924 and 926 through in the first refrigeration system 902.Heat exchanger 920,922,924 and 926 also can be called as evaporimeter, cooler or ice chest.Natural gas flow 918 can be by being cooled with the non-hydrocarbons indirect heat exchange of circulation in each of heat exchanger 920,922,924 and 926.Non-hydrocarbons cold-producing medium can be HFC, for example R-404A or R-410A, or the non-hydrocarbons cold-producing medium of any other applicable type.
Non-hydrocarbons cold-producing medium can cycle through the first refrigeration system 902 continuously, its can be continuously for the preparation of each the non-hydrocarbons cold-producing medium that enters heat exchanger 920,922,924 and 926.Non-hydrocarbons cold-producing medium can be used as steam non-hydrocarbons cold-producing medium and leaves the first heat exchanger 920 via pipeline 928.Steam non-hydrocarbons cold-producing medium can with pipe joint 930 in the combination of extra steam non-hydrocarbons cold-producing medium.Then steam non-hydrocarbons cold-producing medium flows through compressor 932 to increase the pressure of steam non-hydrocarbons cold-producing medium, produces overheated steam non-hydrocarbons cold-producing medium.Superheated steam non-hydrocarbons cold-producing medium flows through condenser 934, and it can be cooling and condensation superheated steam non-hydrocarbons cold-producing medium, produces liquid non-hydrocarbons cold-producing medium.
Liquid non-hydrocarbons cold-producing medium can flow through expansion valve 935, and it reduces the temperature and pressure of liquid non-hydrocarbons cold-producing medium.This can cause the flash distillation of liquid non-hydrocarbons cold-producing medium, produces the mixture of liquid non-hydrocarbons cold-producing medium and steam non-hydrocarbons cold-producing medium.Liquid non-hydrocarbons cold-producing medium and steam non-hydrocarbons cold-producing medium can flow into the first flash drum 936 via pipeline 938.In the first flash drum 936, liquid non-hydrocarbons cold-producing medium can be separated with steam non-hydrocarbons cold-producing medium.
Steam non-hydrocarbons cold-producing medium can flow to pipe joint 930 from the first flash drum 936 via pipeline 940.Liquid non-hydrocarbons cold-producing medium can flow ipe joint 942, and it can separate liquid non-hydrocarbons cold-producing medium is two separated liquid non-hydrocarbons cold-producing mediums streams.A liquid non-hydrocarbons cold-producing medium stream can flow through the first heat exchanger 920, flash-off of steam partially or completely, and turn back to pipe joint 930 via pipeline 928.Another liquid non-hydrocarbons cold-producing medium stream can flow to the second flash drum 944 via pipeline 946.Pipeline 946 also can comprise expansion valve 948, and its throttling liquid non-hydrocarbons cold-producing medium flows to control liquid non-hydrocarbons cold-producing medium stream and flows into the second flash drum 944.The throttling in expansion valve 948 of liquid non-hydrocarbons cold-producing medium stream can cause the flash distillation of liquid non-hydrocarbons cold-producing medium stream, produces the two mixture of steam and liquid non-hydrocarbons cold-producing medium.
The second flash drum 944 can be separated with liquid non-hydrocarbons cold-producing medium by steam non-hydrocarbons cold-producing medium.Steam non-hydrocarbons cold-producing medium can be via pipeline 952 flow ipe joints 950.Pipe joint 950 can combined steam non-hydrocarbons cold-producing medium and the steam non-hydrocarbons cold-producing medium that reclaims from the second and the 3rd heat exchanger 922 and 924.The steam non-hydrocarbons cold-producing medium of combination can be interior compressed at compressor 954, and via pipeline 956 flow ipe joints 930, with the steam combination from flash drum 936 and heat exchanger 920.
Liquid non-hydrocarbons cold-producing medium can flow to pipe joint 958 from the second flash drum 944, and it can separate liquid non-hydrocarbons cold-producing medium is two separated liquid non-hydrocarbons cold-producing medium streams.A liquid non-hydrocarbons cold-producing medium stream flows through the second heat exchanger 922 and turns back to pipe joint 950 via pipeline 960.Another liquid non-hydrocarbons cold-producing medium is flowed through and is flow to the 3rd flash drum 962 by pipeline 964.Pipeline 964 also comprises expansion valve 966, and it is controlled liquid non-hydrocarbons cold-producing medium stream and flows into the 3rd flash drum 962.Expansion valve 966 may cause the flash distillation of liquid non-hydrocarbons cold-producing medium stream, produces the two mixture of steam and liquid non-hydrocarbons cold-producing medium.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 cold-producing medium can flash distillation enter the 3rd flash drum 962, further reduces temperature and pressure.The 3rd flash drum 962 can be separated with liquid non-hydrocarbons cold-producing medium by steam non-hydrocarbons cold-producing medium.Steam non-hydrocarbons cold-producing medium can be via pipeline 970 flow ipe joints 968.Pipe joint 968 can combined steam non-hydrocarbons cold-producing medium and from the third and fourth heat exchanger 924 and the 926 steam non-hydrocarbons cold-producing mediums that reclaim.The steam non-hydrocarbons cold-producing medium of combination can be interior compressed and via pipeline 974 flow ipe joints 950 at compressor 972.
Liquid non-hydrocarbons cold-producing medium can be from the 3rd flash drum 962 flow ipe joints 976, and it can separate liquid non-hydrocarbons cold-producing medium is two separated liquid non-hydrocarbons cold-producing medium streams.A liquid non-hydrocarbons cold-producing medium stream can flow through the 3rd heat exchanger 924 and turn back to pipe joint 968 via pipeline 978.Another liquid non-hydrocarbons cold-producing medium stream can flow through the 4th heat exchanger 926 via pipeline 980.Pipeline 980 also can comprise expansion valve 982, and it allows the flash distillation of liquid non-hydrocarbons cold-producing medium, and therefore, along with it flows into the pressure and temperature that the 4th heat exchanger 926 has reduced liquid non-hydrocarbons cold-producing medium stream.From the 4th heat exchanger 926, liquid non-hydrocarbons cold-producing medium stream can be interior compressed and be sent to pipe joint 968 via pipeline 986 at compressor 984.
In one embodiment, the refrigerant mixture that comprises rare gas by flow through heat exchanger 920,922,924 and 926 each by pre-cooled.As discussed further below, refrigerant mixture can flow to the heat exchanger 920,922,924 and 926 in the first refrigeration system 902 from the second refrigeration system 904 via pipeline 988.
Natural gas flow is by after progressively freezing in each of heat exchanger 920,922,924 and 926, and it flows into the second refrigeration systems 904 via pipeline 990, as shown in Figure 9 B.The second refrigeration system 904 can comprise the 5th heat exchanger 992 and the 6th heat exchanger 994, and it can be used for further cooled natural gas stream.The refrigerant mixture that the 5th heat exchanger 992 and the 6th heat exchanger 994 can utilize and comprise one or more rare gas---for example xenon or krypton---carrys out cooled natural gas stream.
Refrigerant mixture can cycle through the second refrigeration system 904 continuously, and it is for the preparation of each the refrigerant mixture that enters heat exchanger 992 and 994.Refrigerant mixture can be used as vapor refrigerant mixture and leaves the 5th heat exchanger 992 via pipeline 996.Vapor refrigerant mixture can with pipe joint 998 in extra steam refrigerant mixture combination.Then vapor refrigerant mixture can flow through compressor 1000, and the pressure that it can increase vapor refrigerant mixture produces overheated vapor refrigerant mixture.Superheated vapor refrigerant mixture can flow through gas cooler 1002, and it can cooling superheated vapor refrigerant mixture, produces liquid refrigerant mixture.In some cases, if vapor refrigerant mixture lower than room temperature, vapor refrigerant mixture may not flow through gas cooler 1002.As discussed above, then liquid refrigerant mixture can flow through the heat exchanger 920,922,924 and 926 in the first refrigeration system 902 via pipeline 988.
Once refrigerant mixture is through heat exchanger 920,922,924 and 926, refrigerant mixture can enter the 4th flash drum 1004 in the second refrigeration system 904 via pipeline 1006.Pipeline 1006 can comprise expansion valve 1008, and it is controlled refrigerant mixture and flows into the 4th flash drum 1004.Expansion valve 1008 can reduce the temperature and pressure of refrigerant mixture, cause refrigerant mixture flash to vapor refrigerant mixture and liquid refrigerant mixture the two.
Vapor refrigerant mixture and liquid refrigerant mixture can flash distillation enter the 4th flash drum 1004, and it can be separated with liquid refrigerant mixture by vapor refrigerant mixture.Vapor refrigerant mixture can be via pipeline 1010 flow ipe joints 998.Liquid refrigerant mixture can flow to pipe joint 1012 from the 4th flash drum 1004, and it can separate liquid refrigerant mixture is two separated liquid refrigerant mixture streams.A liquid refrigerant mixture stream can flow through the 5th heat exchanger 992 and turn back to pipe joint 998 via pipeline 996.Another liquid refrigerant mixture stream can flow through the 6th heat exchanger 994 via pipeline 1014.Pipeline 1014 also can comprise expansion valve 1016, and it is controlled liquid refrigerant mixture stream and flows into the 6th heat exchanger 994, for example, by making refrigerant mixture flash distillation, reduces temperature, and forms vapor refrigerant mixture and liquid refrigerant mixture.From the 6th heat exchanger 994, the vapor refrigerant mixture of gained can be interior compressed at compressor 1018, and then flow ipe joint 998 recycles.
After natural gas flow has been cooled by the refrigerant mixture indirect heat exchange with comprising one or more rare gas in heat exchanger 992 and 994, natural gas flow can flow into from refrigeration system 1000, as shown in figure 10 via pipeline 1020.From refrigeration system 1000, can comprise the various parts for liquefied natural gas, produce LNG.
Natural gas flow can flow ipe joint 1022, and it can combine from the natural gas flow of pipeline 1020 and a part of natural gas flow 916.Before natural gas via is by pipeline 1026 flow ipe joints 1022, the initial cooling of natural gas can carry out in heat exchanger 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 in the interior expansion of hydraulic buckling turbine 1030, and then via pipeline 1034, flows into NRU systems 1032 to remove excessive nitrogen from natural gas.In a plurality of embodiments, natural gas flows into the low-temperature fractionation tower 1036 in NRU system 1032, for example NRU tower.In addition, heat can be transferred to low-temperature fractionation tower 1036 via pipeline 1037 from reboiler 1028.
Low-temperature fractionation tower 1036 can be separated with natural gas by nitrogen via cryogenic distillation method.Overhead stream can flow out low-temperature fractionation tower 1036 via pipeline 1038.Overhead stream can mainly comprise methane and low boiling or non-condensable gas, for example nitrogen and helium, and it is separated with natural gas.Overhead stream can flow into overhead condenser 1040, its any liquid in can separated overhead stream, and using it as backflow, turn back to low-temperature fractionation tower 1036.This may cause another vapor stream that produces a vapor stream, mainly comprises the fuel flow of methane and mainly comprise low-boiling point gas.Fuel flow can flow through heat exchanger 1024 via pipeline 1042.In heat exchanger 1024, the temperature of vapor fuel stream can increase via the indirect heat exchange with natural gas flow 916, produces vapor fuel stream.Vapor fuel stream then can be interior compressed at compressor 1044, and via pipeline 1048, flow out cascade cooling system 900 as fuel 1046.From the liquid stream of overhead condenser 1040, can be used as reflow stream and turn back to low-temperature fractionation tower 1036.
Tower base stream in the 1036 interior generations of low-temperature fractionation tower mainly comprises the natural gas with trace nitrogen.Tower base stream and can flow into the 5th flash drum 1049 via pipeline 1050 and 1052 respectively from the vapor stream of overhead condenser 1040.Pipeline 1050 also can comprise expansion valve 1054, and its control tower bottoms stream flows into the 5th flash drum 1049, allows the liquid flashes from a part for tower base stream, forms the mixed phase flow that flows into the 5th flash drum 1049.
In addition, the tower base stream of some parts can flow through overhead condenser 1040 via pipeline 1055.Pipeline 1055 also can comprise expansion valve 1056, and its control tower bottoms stream flows into overhead condenser 1040.Tower base stream can be as the cold-producing medium of overhead condenser 1040.The steam that leaves overhead condenser 1040 of gained can turn back to the 5th flash drum 1049 via pipeline 1052.
The 5th flash drum 1049 can flow for mainly comprising vapor stream and the LNG of natural gas by separated multi-phase flow.Vapor stream can be via pipeline 1060 flow ipe joints 1058.Pipe joint 1058 can combined steam stream and another vapor stream of reclaiming from the 6th flash drum 1062.The vapor stream of combination can be interior compressed at compressor 1064, and the pipe joint 912 flowing in the first refrigeration system 902 via pipeline 1066..
LNG stream can flow into the 6th flash drum 1062 via pipeline 1068.Pipeline 1068 can comprise expansion valve 1070, and it is controlled LNG stream and flows into the 6th flash drum 1062, allows the liquid flashes from a part for LNG stream, forms the mixing phase system that flows into the 6th flash drum 1062.
The 6th flash drum 1062 can separated mixed phase flow be LNG and the vapor stream that comprises natural gas.Vapor stream can be via pipeline 1074 flow ipe joints 1072.Pipe joint 1072 can combined steam stream and another vapor stream of reclaiming from the 7th flash drum 1076.The vapor stream of combination can be at the interior compressed and flow ipe joint 1058 of compressor 1078.
Then LNG stream can flow into the 7th flash drum 1076 via pipeline 1080.Pipeline 1080 can comprise expansion valve 1082, and it is controlled LNG stream and flows into the 7th flash drum 1076, allows the liquid flashes from a part of LNG.The 7th flash drum 1076 can further reduce the temperature and pressure of LNG stream, makes LNG stream approach equilibrium temperature and pressure, as discussed about Figure 11 below.The vapor stream producing can flow ipe joint 1084, and it can combined steam stream and the boil-off gas that reclaims from LNG tank 1086.The vapor stream of combination can be at the interior compressed and flow ipe joint 1072 of compressor 1088.
LNG tank 1086 can be stored LNG stream and continue section any time.Boil-off gas in the 1086 interior generations of LNG tank can be via pipeline 1090 flow ipe joints 1084.Point at any time, LNG stream can be used pump 1094 to be transported to LNG oil truck (tanker) 1092, for being transported to market.The extra boil-off gas 1098 producing when LNG stream is loaded into LNG oil truck 1092 can be by being added pipe joint 1084 to reclaim in cascade cooling system 900.
The process chart that is to be understood that Fig. 9 A, 9B and 10 is not intended to show cascade cooling system 900 and comprises all parts shown in Fig. 9 A, 9B and 10 from refrigeration system 1000.And, according to the details of concrete enforcement, cascade cooling system 900 and/or can comprise unshowned any amount of additional components in Fig. 9 A, 9B and 10 from refrigeration system 1000.For example, in some embodiments, cascade cooling system 900 comprises one or more refrigeration systems of the cold-producing medium that utilizes the single mixing that comprises at least one rare gas.Yet, cascade cooling system 900 and/or also can comprise the combination of refrigeration system or the refrigeration system of any other type from refrigeration system 1000.
Figure 11 is the schematic diagram of pressure of methane-enthalpy (P-H) Figure 110 0.P-H Figure 110 0 shows corresponding pressure 1102 and the enthalpy 1104 at each temperature.The entry of identical numbering is as described about Fig. 9.P-H Figure 110 0 comprises 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.In addition, if the pressure of methane 1102 and enthalpy 1104 in the profile of equilibrium 1106, methane exists as the equilibrium mixture of liquids and gases.If the pressure of methane 1102 and enthalpy 1104 are at the profile of equilibrium more than 1106, methane is in critical condition.
According to described herein, from freezing method, the temperature and pressure 1102 that expectation reduces methane makes methane exist as the liquid that approaches atmospheric pressure.Expansion valve 1056,1070 and 1080 and flash drum 1049,1062 and 1076 in each flash process constant enthalpy ground reduced the temperature and pressure of methane.For example, before passing the expansion of hydraulic buckling turbine 1030, methane can be in critical condition 1112.In many cases, use typical hydrocarbon coolant for example methane be difficult to the critical condition that reaches such.Therefore, in some cases, xenon replaces methane to can be used for from freezing method.
Hydraulic buckling turbine 1030 can reduce temperature and pressure 1102 to first equilibrium states 1114 of methane constant enthalpy.NRU can or operate at the first equilibrium state 1114 under higher a little pressure.The first equilibrium state 1114 can comprise large liquid part 1116 and little gas part 1118.Gas can be discharged the 5th flash drum 1049, makes methane in first pure liquid 1120.Yet first pure liquid 1120 can be in being significantly higher than the pressure 1102 times of atmospheric pressure.Therefore, methane can flow through expansion valve 1070 and enter the 6th flash drum 1062.
Expansion valve 1070 can reduce temperature and pressure 1102 to second equilibrium states 1122 of methane constant enthalpy.Be similar to the first equilibrium state 1118, the second equilibrium states 1122 and can comprise large liquid part and little gas part.Gas can be discharged the 6th flash drum 1062, makes methane in second pure liquid 1124.Yet, second pure liquid 1124 can be still in being significantly higher than the pressure 1102 times of atmospheric pressure.Therefore, methane can flow through expansion valve 1080 and enter the 7th flash drum 1076.
The temperature and pressure 1102 that expansion valve 1082 can reduce methane constant enthalpy is to the 3rd equilibrium state 1126.The 3rd equilibrium state 1126 can comprise large liquid part and little gas part.Gas can be discharged the 7th flash drum 1076, makes methane in the 3rd pure liquid 1128.In a plurality of embodiments, the 3rd pure liquid 1128 pressure 1102 can approach atmospheric pressure.Therefore, methane can be the form of final products, and can be used as LNG output.
lNG formation method
Figure 12 is the process chart that is used to form the method 1200 of LNG.In a plurality of embodiments, method 1200 can in officely how go up in the system 800,900 or 1000 of describing respectively about Fig. 8,9 or 10 and implement.
Method 1200 starts at square 1202, at this natural gas, in refrigeration system, is frozen.Refrigeration system can be mechanical refrigeration system, valve expansion system, turbine expansion system or analog.Refrigeration system is used the refrigerant mixture that comprises rare gas.Rare gas can comprise xenon, krypton, argon or its any combination.In addition, refrigerant mixture can comprise nitrogen or hydrocarbon, for example methane, ethane, propane or butane.According to embodiment described herein, the refrigerant mixture that comprises rare gas for any amount of cooling stage so that provide than hydrocarbon coolant darker cooling to be provided.
In a plurality of embodiments, refrigerant mixture is compressed so that the refrigerant mixture of compression to be provided, and the refrigerant mixture of compression is by being cooled with cooling fluid indirect heat exchange.The refrigerant mixture of compression can be inflated the refrigerant mixture with cooled compressed, thereby produces refrigerant mixture that expand, cooling.Expand, cooling refrigerant mixture can forward heat exchange area to, it can comprise, for example cooler or evaporimeter.In addition, natural gas can be by compressed and cooling with external refrigeration fluid indirect heat exchange.Then natural gas can be used the cooling refrigerant mixture expanding to carry out freezing in heat exchange area.
It is freezing that natural gas can be used the first refrigerant mixture to carry out via one or more pre-cooled steps.The first refrigerant mixture can comprise rare gas, nitrogen or hydrocarbon, or its any combination.Natural gas also can be used second refrigerant mixture to carry out freezing via one or more degree of depth cooling steps.Second refrigerant mixture can comprise rare gas, nitrogen or hydrocarbon, or its any combination.
At square 1204 places, natural gas is being liquefied to form LNG in refrigeration system.In a plurality of embodiments, from refrigeration system, comprise for cooling and a plurality of expansion valves and flash drum liquefied natural gas.Natural gas can pass expansion valve flash distillation, has reduced the pressure and temperature of natural gas, and produces steam cut and liquid distillate.Steam cut and liquid distillate can be flashed and enter flash drum, and it can be separated with liquid distillate by steam cut.This process can repeat in any amount of expansion valve and flash drum, until the natural gas of appropriate amount has been converted into LNG.
The process chart that is to be understood that Figure 12 is not intended to show that the step of method 1200 carries out with any specific order, or all steps all comprise in each case.And according to the details of concrete enforcement, any amount of extra step can be included in method 1200.For example, in refrigeration system, before cooled natural gas, natural gas can be cooled in the first refrigeration system.In a plurality of embodiments, the first refrigeration system is used non-hydrocarbons cold-producing medium.
Claims (33)
1. the system that is used to form liquefied natural gas (LNG), comprising:
Refrigeration system, it is configured to use the freezing natural gas of refrigerant mixture that comprises rare gas; With
From refrigeration system, its be configured to use described natural gas as self-cold-producing medium to be to form described LNG by described natural gas.
2. system according to claim 1, comprises the first refrigeration system, and it is configured to use natural gas described in non-hydrocarbons refrigerant cools before described natural gas flows into described refrigeration system.
3. system according to claim 1, comprises the described nitrogen gas recovering apparatus from refrigeration system upstream.
4. system according to claim 1, wherein said system configuration, with freezing described natural gas, is controlled for hydrocarbon dew point.
5. system according to claim 1, wherein said system configuration, with freezing described natural gas, is extracted for natural gas liquids (NGL).
6. system according to claim 1, wherein said system configuration with by methane with separated with heavier gas with carbon dioxide compared with lighter-than-air gas.
7. system according to claim 1, wherein said system configuration is with the hydrocarbon for the preparation of liquefied petroleum gas (LPG) production inventory.
8. system according to claim 1, wherein said system configuration flows with condensing reflux.
9. system according to claim 1, wherein said refrigerant mixture comprises xenon or krypton, or its any combination.
10. system according to claim 1, wherein said refrigerant mixture comprises xenon, krypton, argon or nitrogen, or its any combination.
11. systems according to claim 1, wherein said refrigeration system comprises mechanical refrigeration system, valve expansion system or turbine expansion system, or its any combination.
12. systems according to claim 1, wherein said refrigerant mixture comprises hydrocarbon, and wherein said hydrocarbon comprises methane, ethane, propane or butane, or its any combination.
13. systems according to claim 1, wherein said refrigeration system comprises a plurality of cool cycles.
14. systems according to claim 1, wherein said refrigeration system comprises a plurality of cool cycles, it comprises:
In one or more pre-cooled stages, wherein said refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination, and
One or more degree of depth cool cycles, wherein said refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination.
15. systems according to claim 1 wherein utilize the described refrigerant mixture comprise described rare gas so that the cooling of the more degree of depth that provides than hydrocarbon coolant to be provided in one or more cooling stages.
16. systems according to claim 1, comprise nitrogen rejection facility, wherein use liquid charging stock from the bottom of described nitrogen rejection facility so that the reflux condenser being cooled at the top of described nitrogen rejection facility to be provided.
17. systems according to claim 1, wherein said refrigerant mixture comprises pure component refrigerants.
18. are used to form the method for liquefied natural gas (LNG), comprising:
Freezing natural gas in refrigeration system, wherein said refrigeration system is used the refrigerant mixture that comprises rare gas; With
At the described natural gas that liquefies in refrigeration system to form described LNG.
19. methods according to claim 18, are included in described refrigeration system before freezing described natural gas cooling described natural gas in the first refrigeration system, and wherein said the first refrigeration system is used non-hydrocarbons cold-producing medium.
20. methods according to claim 18, wherein in described refrigeration system, freezing described natural gas comprises:
Compress described refrigerant mixture so that the refrigerant mixture of compression to be provided;
Optionally, by the refrigerant mixture with the cooling described compression of cooling fluid indirect heat exchange;
Expand the refrigerant mixture of described compression with the refrigerant mixture of cooling described compression, thereby produce refrigerant mixture that expand, cooling;
Make refrigerant mixture described expansion, cooling go to the first heat exchange area;
Optionally, compress described natural gas;
Optionally, by with the cooling described natural gas of external refrigeration fluid indirect heat exchange; With
Make refrigerant mixture heat exchange described natural gas and described expansion, cooling.
21. methods according to claim 18, wherein said rare gas comprises xenon or krypton.
22. methods according to claim 18, wherein said refrigerant mixture comprises nitrogen or hydrocarbon, or its any combination.
23. methods according to claim 18, comprise via a plurality of expansion valves or hydraulic buckling turbine and flash drum and liquefy described natural gas to form described LNG.
24. methods according to claim 18, comprising:
Via one or more pre-cooled steps, use the freezing described natural gas of the first refrigerant mixture, wherein said the first refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination, and
Via one or more degree of depth cooling steps, use the freezing described natural gas of second refrigerant mixture, wherein said second refrigerant mixture comprises rare gas, nitrogen or hydrocarbon, or its any combination.
25. methods according to claim 18, are included in one or more cooling stages and use the described refrigerant mixture that comprises described rare gas so that the cooling of the more degree of depth that provides than hydrocarbon coolant to be provided.
26. are used to form the cascade cooling system of liquefied natural gas (LNG), comprising:
The first refrigeration system, it is configured to use natural gas described in non-hydrocarbons refrigerant cools, wherein said the first refrigeration system comprises a plurality of the first coolers, and it is configured to allow via the cooling described natural gas of indirect heat exchange between described natural gas and described non-hydrocarbons cold-producing medium;
The second refrigeration system, it is configured to use the freezing described natural gas of refrigerant mixture that comprises rare gas, wherein said the second refrigeration system comprises a plurality of the second coolers, and it is configured to allow via the cooling described natural gas of the indirect heat exchange between described natural gas and described refrigerant mixture; With
From refrigeration system, it is configured to form described LNG from described natural gas, wherein saidly from refrigeration system, comprises a plurality of expansion valves or hydraulic buckling turbine, or its any combination, and flash drum.
27. cascade cooling systems according to claim 26, wherein said the first refrigeration system comprises compressor and condenser, and described compressor configuration is to compress described non-hydrocarbons cold-producing medium, and described condenser arrangement is with cooling described non-hydrocarbons cold-producing medium.
28. cascade cooling systems according to claim 26, wherein said the second refrigeration system comprises compressor and condenser, and described compressor configuration is to compress described refrigerant mixture, and described condenser arrangement is with cooling described refrigerant mixture.
29. cascade cooling systems according to claim 26, wherein said a plurality of the first cooler comprises evaporimeter, and it is configured to by the cooling described natural gas via heat being transferred to from described natural gas to the described non-hydrocarbons cold-producing medium described non-hydrocarbons cold-producing medium of at least part of vaporization.
30. cascade cooling systems according to claim 26, wherein said a plurality of the second cooler comprises evaporimeter, and it is configured to by via heat being transferred to from described natural gas to described refrigerant mixture vaporize described refrigerant mixture and freezing described natural gas.
31. cascade cooling systems according to claim 26, wherein said LNG comprises liquid distillate and residue vapor cut, and wherein said cascade cooling system comprises fluid separation applications container, it is configured to described residue vapor cut separated with described liquid distillate.
32. cascade cooling systems according to claim 26, comprise the described nitrogen rejection facility from refrigeration system upstream.
33. cascade cooling systems according to claim 26, wherein said refrigerant mixture comprises pure component refrigerants.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
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| 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 |
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| CN104204698A true CN104204698A (en) | 2014-12-10 |
| CN104204698B CN104204698B (en) | 2017-09-08 |
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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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| 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) |
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| SG11201504193VA (en) * | 2013-01-24 | 2015-08-28 | Exxonmobil Upstream Res Co | Liquefied natural gas production |
| 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 |
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| 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 |
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Also Published As
| Publication number | Publication date |
|---|---|
| CA2867436C (en) | 2019-04-09 |
| AR090506A1 (en) | 2014-11-19 |
| CA2867436A1 (en) | 2013-10-03 |
| EP2831523A4 (en) | 2016-08-10 |
| CN104204698B (en) | 2017-09-08 |
| 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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