CN104813127B - The liquefaction of natural gas - Google Patents
The liquefaction of natural gas Download PDFInfo
- Publication number
- CN104813127B CN104813127B CN201380059674.2A CN201380059674A CN104813127B CN 104813127 B CN104813127 B CN 104813127B CN 201380059674 A CN201380059674 A CN 201380059674A CN 104813127 B CN104813127 B CN 104813127B
- Authority
- CN
- China
- Prior art keywords
- fluorocarbons
- refrigerant
- refrigeration system
- natural gas
- nitrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 593
- 239000003345 natural gas Substances 0.000 title claims abstract description 263
- 239000003507 refrigerant Substances 0.000 claims abstract description 488
- 238000005057 refrigeration Methods 0.000 claims abstract description 310
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 296
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 141
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 125
- 238000000034 method Methods 0.000 claims abstract description 102
- 238000001816 cooling Methods 0.000 claims description 138
- 229930195733 hydrocarbon Natural products 0.000 claims description 112
- 150000002430 hydrocarbons Chemical class 0.000 claims description 111
- 239000004215 Carbon black (E152) Substances 0.000 claims description 110
- 239000007789 gas Substances 0.000 claims description 84
- 238000012545 processing Methods 0.000 claims description 74
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 52
- 238000007906 compression Methods 0.000 claims description 46
- 230000006835 compression Effects 0.000 claims description 45
- 239000012809 cooling fluid Substances 0.000 claims description 18
- PRPAGESBURMWTI-UHFFFAOYSA-N [C].[F] Chemical compound [C].[F] PRPAGESBURMWTI-UHFFFAOYSA-N 0.000 claims description 17
- 239000003795 chemical substances by application Substances 0.000 claims description 15
- 231100000252 nontoxic Toxicity 0.000 claims description 2
- 230000003000 nontoxic effect Effects 0.000 claims description 2
- 239000007788 liquid Substances 0.000 description 110
- -1 perfluorocarbon compound Chemical class 0.000 description 56
- 230000008569 process Effects 0.000 description 47
- 239000000203 mixture Substances 0.000 description 43
- 239000000463 material Substances 0.000 description 26
- 150000001875 compounds Chemical class 0.000 description 20
- 238000003860 storage Methods 0.000 description 19
- 229910052731 fluorine Inorganic materials 0.000 description 17
- 235000019000 fluorine Nutrition 0.000 description 16
- 229910052799 carbon Inorganic materials 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 15
- 239000011737 fluorine Substances 0.000 description 15
- 238000005194 fractionation Methods 0.000 description 15
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 14
- 238000002360 preparation method Methods 0.000 description 14
- 238000011144 upstream manufacturing Methods 0.000 description 14
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 12
- 238000009835 boiling Methods 0.000 description 10
- 239000002826 coolant Substances 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 9
- UGCSPKPEHQEOSR-UHFFFAOYSA-N 1,1,2,2-tetrachloro-1,2-difluoroethane Chemical compound FC(Cl)(Cl)C(F)(Cl)Cl UGCSPKPEHQEOSR-UHFFFAOYSA-N 0.000 description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 238000003763 carbonization Methods 0.000 description 7
- 239000000470 constituent Substances 0.000 description 7
- 239000000446 fuel Substances 0.000 description 7
- 239000003915 liquefied petroleum gas Substances 0.000 description 7
- 239000011555 saturated liquid Substances 0.000 description 7
- 150000001335 aliphatic alkanes Chemical class 0.000 description 6
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 238000000605 extraction Methods 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- GTLACDSXYULKMZ-UHFFFAOYSA-N pentafluoroethane Chemical compound FC(F)C(F)(F)F GTLACDSXYULKMZ-UHFFFAOYSA-N 0.000 description 6
- 239000001294 propane Substances 0.000 description 6
- 230000009467 reduction Effects 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 238000010025 steaming Methods 0.000 description 6
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 5
- 230000008859 change Effects 0.000 description 5
- 238000013461 design Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 238000007701 flash-distillation Methods 0.000 description 5
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 5
- 238000007710 freezing Methods 0.000 description 5
- 230000008014 freezing Effects 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000001273 butane Substances 0.000 description 4
- 150000001721 carbon Chemical group 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- RWRIWBAIICGTTQ-UHFFFAOYSA-N difluoromethane Chemical compound FCF RWRIWBAIICGTTQ-UHFFFAOYSA-N 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 125000001153 fluoro group Chemical group F* 0.000 description 4
- 239000001307 helium Substances 0.000 description 4
- 229910052734 helium Inorganic materials 0.000 description 4
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000009834 vaporization Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 229910001868 water Inorganic materials 0.000 description 4
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 150000001722 carbon compounds Chemical class 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 210000003205 muscle Anatomy 0.000 description 3
- 150000002829 nitrogen Chemical class 0.000 description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 239000000498 cooling water Substances 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
- 239000003502 gasoline Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 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
- QGHDLJAZIIFENW-UHFFFAOYSA-N 4-[1,1,1,3,3,3-hexafluoro-2-(4-hydroxy-3-prop-2-enylphenyl)propan-2-yl]-2-prop-2-enylphenol Chemical group C1=C(CC=C)C(O)=CC=C1C(C(F)(F)F)(C(F)(F)F)C1=CC=C(O)C(CC=C)=C1 QGHDLJAZIIFENW-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-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
- 230000009471 action Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 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
- 230000033228 biological regulation Effects 0.000 description 1
- 238000005219 brazing Methods 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000012993 chemical processing Methods 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 150000002222 fluorine compounds Chemical class 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000010582 gas stream method Methods 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
- 230000008676 import Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- MSSNHSVIGIHOJA-UHFFFAOYSA-N pentafluoropropane Chemical compound FC(F)CC(F)(F)F MSSNHSVIGIHOJA-UHFFFAOYSA-N 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000007639 printing Methods 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
- 238000007670 refining Methods 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 230000026676 system process Effects 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
- 239000004408 titanium dioxide Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—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"
- F25J1/0045—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 vaporising a liquid return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0207—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 as at least a three level SCR refrigeration cascade
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—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
- F25J1/0217—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle
- F25J1/0218—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle with one or more SCR cycles, e.g. with a C3 pre-cooling cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—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
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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Abstract
The invention discloses the system and method for forming liquefied natural gas (LNG).The system includes being configured so that the first fluorocarbons refrigeration system of the first fluorocarbons refrigerant chilling natural gas and is configured so that the second fluorocarbons refrigeration system of the further chilling natural gas of the second fluorocarbons refrigerant.The system also includes being configured so that refrigerant cooled natural gas the nitrogen deliverying unit to prepare the nitrogen refrigeration system of LNG and be configured to be removed from LNG nitrogen.The alternatively embodiment of property, the nitrogen refrigeration system can be replaced by methane from refrigeration system.
Description
Cross-Reference to Related Applications
U.S. this application claims entitled " liquefaction of natural gas " of benefiting from the submission of on November 16th, 2012 is temporarily special
Profit application 61/727,577, entire contents are incorporated herein by reference to document.
Invention field
Technology of the invention relates generally to the field of hydrocarbon recovery and processing method, and relates more specifically to the method by freezing
The method and system of liquefied natural gas (LNG) is formed, it is included in nitrogen kind of refrigeration cycle or methane from the two of kind of refrigeration cycle upstream
Individual fluorocarbons kind of refrigeration cycle.
Background technology
This part is intended to introduce many aspects of prior art, and it can be with the exemplary of the technology of the present invention
It is related.Believe the framework of the special aspects that this content of the discussions contributes to provides convenient to be better understood from the technology of the present invention.Therefore,
It should be appreciated that this part content should be read based on this point, and there is no need as prior art
Statement.
Many all relies on the refrigeration including hydrocarbon component and nitrogen for natural gas processing and liquefied cryogenic refrigerating system
The use of agent is to provide external refrigeration.These hydrocarbon components can include methane, ethane, ethene, propane and similar material.So
And, in many cases, it may be desirable that implement refrigeration system using non-combustible refrigerant.
The U.S. patents No.6,412,302 of Foglietta et al. describes a kind of side for preparing liquefied natural gas stream
Method.The method includes being exchanged heat and being cooled down by the refrigerant contact with the first and second expansions circulated for independent cooling
The natural gas feed stream of at least a portion pressurization.First expanding refrigerant is selected from methane, ethane and the day for processing and pressurizeing
Right gas, and the second expanding refrigerant is nitrogen.But, as being discussed in the present invention, expect to prepare and freezed using non-combustible
LNG stream inside the refrigeration system of agent.
Summary of the invention
One embodiment of the invention provides a kind of hydrocarbon system of processing for forming liquefied natural gas (LNG).Should
Hydrocarbon system of processing includes being configured so that the first fluorocarbons refrigeration system of the first fluorocarbons refrigerant chilling natural gas
Unite and be configured so that the second fluorocarbons refrigeration system of the further chilling natural gas of the second fluorocarbons refrigerant.Should
Hydrocarbon system of processing also includes being configured so that nitrogen gas refrigerant cooled natural gas preparing the nitrogen refrigeration system of LNG and being configured to
The nitrogen deliverying unit of nitrogen is removed from LNG.
Another embodiment of the invention provides a kind of method of formation LNG.The method is included in the carbonization of the first fluorine
Cooled natural gas in compound refrigeration system, in the second fluorocarbons refrigeration system cooled natural gas, in nitrogen refrigeration system
Middle liquefied natural gas is forming LNG and in nitrogen deliverying unit nitrogen be removed from LNG.
Another embodiment of the invention provides a kind of hydrocarbon system of processing for forming LNG.The hydrocarbon system of processing
The first refrigeration system including being configured so that the first fluorocarbons refrigerant cooled natural gas, wherein first refrigeration system
It is configured to allow by the indirect heat exchange between natural gas and the first fluorocarbons refrigerant cooled natural gas including many
First Heat Exchanger.The hydrocarbon system of processing includes being configured so that the second system of the second fluorocarbons refrigerant chilling natural gas
Cooling system, wherein second refrigeration system including many be configured to allow by natural gas and the second fluorocarbons refrigerant it
Between indirect heat exchange and the second heat exchanger of cooled natural gas.The hydrocarbon system of processing also include be configured so that nitrogen gas refrigerant by
3rd refrigeration system of natural gas adsorption LNG, wherein the 3rd refrigeration system be configured to allow by natural gas including many and
Indirect heat exchange between nitrogen gas refrigerant and the 3rd heat exchanger of cooled natural gas.The hydrocarbon system of processing still further comprises configuration
It is the nitrogen deliverying unit that nitrogen is removed from LNG.
Another embodiment of the invention provides a kind of hydrocarbon system of processing of formation LNG.The hydrocarbon system of processing includes
The first fluorocarbons refrigeration system of the first fluorocarbons refrigerant chilling natural gas is configured so that, is configured so that
Second fluorocarbons refrigeration system of the further chilling natural gas of two fluorocarbons refrigerants, and it is configured to cooling naturally
Gas is preparing the methane of LNG from refrigeration system.
Summary of drawings
The advantage of the technology of the present invention can be better understood from by reference to the following detailed description and accompanying drawing, wherein：
Fig. 1 is the process chart of single phase refrigeration system；
Fig. 2 is the process chart for including the two benches refrigeration system for saving device；
Fig. 3 is to include that heat exchanger saves the process chart of the single phase refrigeration system of device；
Fig. 4 is the process chart of the cascade cooling system for including the first refrigeration system and the second refrigeration system；
Fig. 5 is the process chart of the expansion refrigeration system for hydrocarbon dew point control；
Fig. 6 is the process chart of the expansion refrigeration system prepared for NGL；
Fig. 7 is the process chart of LNG preparation systems；
Fig. 8 A and 8B are the process charts of the cascade fluorocarbons cooling system with nitrogen refrigeration；
Fig. 9 is the process chart for including the system of NRU；
Figure 10 A and 10B are the process charts for cascading fluorocarbons cooling system that there is nitrogen to freeze for another；
Figure 10 C are with nitrogen refrigeration cooling system and the cascade fluorocarbons cooling system for simplifying nitrogen refrigeration system
A process chart for selective embodiment；
Figure 11 A and 11B are the process charts of another cascade cooling system；
Figure 11 C are implemented in the cascade cooling system identical hydrocarbon system of processing with Figure 11 A and 11B from refrigeration system
Process chart；
Figure 12 is the process chart of the method by natural gas adsorption LNG；And
Figure 13 is by the process chart of another method of natural gas adsorption LNG.
Detailed description of the invention
The specific embodiment of the technology of the present invention is described in part described in detail below.However, right from following description
For the particular embodiment of the technology of the present invention and the aspect of specific use, it is meant only to exemplary purpose and typically carries
For the description of exemplary.Therefore, the technology is not limited to the specific embodiment of present invention description, but including falling
Enter all alternatives in the spirit and scope of appended claims, improved form and the equivalent form of value.
Firstly, for the item of reference, some are used for the term and their implication of the application and are used for the present invention up and down
Text equally sets.When not defined in the present invention for term of the invention, should be according at least one printing
Publication or publication patent provide the related art for reflecting in those skilled in the art assign the most wide of the term
The definition of justice.Additionally, the technology of the present invention is not by the term, and shown usage is limited in the present invention, its all of shape of equal value
Formula, synonym, new development and term or technology for same or similar purpose all think it in claims of the present invention
In the range of.
Just as used in the present invention, a part of product stream is referred to for the method for purpose of freezing " from freezing ".This
Implemented by extracting a part of product stream based on the purpose for providing refrigeration capacity before final cooling.This extraction
Logistics expands in valve or expander, and as the result of expansion, the temperature drop of logistics.This logistics is changed for cooling
Product stream in hot device.After heat exchange, this logistics again second compression and with feed gas stream be blended.This method is also
Know for open cycle is freezed.
Alternatively, liquid is referred to by reducing the method that thus pressure cool down " from freezing ".In the case of liquid, from
Refrigeration is referred to by evaporative cooling liquid body, its reduction for corresponding to pressure.More particularly, when the liquid of a part is through section
The liquid flashes of the part are steam during the reduction of experience pressure while stream device.As a result, the liquid of steam and residual
Both it is cooled to the saturation temperature under the pressure of reduction.For example, according to the embodiment of present invention description, the self-control of natural gas
It is cold to carry out being cooled down with the loss of heat during vaporizing so as to natural gas by making natural gas be maintained at boiling point.This
The method of kind also refers to " flash distillation ".
Just as used in the present invention, " cascade cycle " refers to the system with two or more refrigerants, wherein cold
Second refrigerant condensed by warmer the first refrigerant.Therefore, low temperature can be by a kind of refrigerant and another " level
Connection " gets up.Based on the pressure for saving stepped evaporation in device, the every kind of refrigerant in cascade can be provided with multiple chilled water (chw)
It is flat.Compared with single refrigeration system, cascade cycle is considered as preparing LNG being favourable, because in cascade cycle
It is middle more to obtain relatively low temperature than single refrigeration system.
" compressor " or " coolant compressor " includes that any unit of refrigerant stream pressure, device can be increased or sets
It is standby.This includes the coolant compressor with independent compression process or step, or the system with multistage compression or step
Refrigerant compressor, more particularly the multistep coolant compressor in individually packaging or shell.The refrigeration of evaporation to be compressed
Agent logistics can be supplied to coolant compressor with different pressure.Some stages of hydrocarbon cooling procedure or step can be included simultaneously
Two or more coolant compressors of connection, series connection or both sides.The present invention is not by coolant compressor, particularly any system
The limitation of the type of refrigerant circuit or arrangement or design.
Just as used in the present invention, " cooling " mean broadly that make the temperature of material and/or interior energy reduce and/or under
Drop, such as any suitable amount.Cooling can include at least about 1 DEG C, at least about 5 DEG C, at least about 10 DEG C, at least about
15 DEG C, at least about 25 DEG C, at least about 50 DEG C, at least about 100 DEG C or similar temperature drop.Cooling can use any
Suitable radiator, such as steam generation, hot water heating, cooling water, air, refrigerant, other process-streams (integration) and
Their joint.One or more cooling source can combine and/or cascade to reach desired output temperature.Cooling step can be with
Use the cooling unit with any appropriate device and/or equipment.According to an embodiment, cooling can include changing indirectly
Heat, such as with one or more heat exchangers.Heat exchanger can include any suitable design, such as shell-and-tube, brazed aluminum formula,
Spiral wound and/or similar designs.In the scheme of selectivity, cooling can be cooled down using evaporation (heat of vaporization), and sensible heat is cold
But, and/or direct heat transfer, for example by liquid Direct spraying to process-stream.
" cryogenic temperature " refers to about -50 DEG C or lower temperature.
Just as used in the present invention, term " dethanizer " and " domethanizing column " refer to can be used for separating natural gas
The distillation column or destilling tower of component in logistics.For example, domethanizing column is used for methane and other volatile components and ethane and weight
Matter Component seperation.The typical conduct of methane fraction contains a small amount of inert gas, such as nitrogen, CO2Or the purified gas of similar gas
Body is reclaimed.
" fluorocarbons " also refers to " perfluorocarbon compound " or " PFC ", and it is the molecule for including F and C atoms.Fluorine carbon
Compound has F-C keys, and depending on the number of carbon atom in species, C-C keys.The example of fluorocarbons includes hexafluoro second
Alkane (C2F6)." HFC " or " HFC " is the fluorocarbons including H, F and C atom of specific type.HFC
Compound has H-C and F-C keys, and depending on the number of carbon atom in species, C-C keys.Some examples of HFC
Including fluoroform (CHF3), pentafluoroethane (C2HF5), HFC-134a (C2H2F4), heptafluoro-propane (C3HF7), HFC-236fa (C3H2F6)、
Pentafluoropropane (C3H3F5) and tetrafluoropropane (C3H4F4), in addition there is the compound of similar chemical constitution.
Term " gas " and " steam " used interchangeably, and it is defined as the gas shape that is distinguished with liquid or solid state
The material of state or the mixture of material.Likewise, term " liquid " represents the liquid condition distinguished with gas or solid state
Material or material mixture.
A kind of any device that heat can be delivered to another medium from medium of expression of " heat exchanger " broad sense, it includes
Any special structure, for example, be commonly referred to as the device of heat exchanger.Heat exchanger includes " direct heat exchanger " and " indirect heat exchange
Device ".Therefore, heat exchanger can be shell-tubular type, spiral, hairpin formula, core type, core-autoclave, double hose, brazed aluminum formula,
Spiral wound or heat exchanger known to any other type." heat exchanger " also refer to any post, tower, unit or other be adapted to
Allow one or more logistics to extend therethrough, and carry out one or more refrigeration lines and one or more feed stream it
Between directly or indirectly heat exchange other arrangement.
" hydrocarbon " is mainly to include the organic compound of element hydrogen and carbon, although nitrogen, sulphur, oxygen, metal or it is any number of its
He can also exist element on a small quantity.Just as used in the present invention, hydrocarbon is commonly referred to as in natural gas, oil or chemical processing plant (CPP)
It was found that component.
" liquefied natural gas " or " LNG " is the commonly known natural gas including high percentage methane.However, LNG can be with
Other compounds including trace.Other elements or compound can include but is not limited to ethane, propane, butane, titanium dioxide
They are processed to remove one or more component (such as helium by carbon, nitrogen, helium, hydrogen sulfide or their joint
Gas) or impurity (such as water and/or heavy hydrocarbon), and under almost atmospheric pressure liquid is condensed into by cooling afterwards.
" liquefied petroleum gas " or " LPG " is commonly referred to as the propane derived from refining crude oil, butane or other light hydrocarbons
Mixture.At a normal temperature, LPG is gas.However, LPG can be cooled down or be pressurizeed to facilitate storage and transport.
" mixed refrigerant process " can be included but is not limited to using the independent system of mix refrigerant, i.e., with more than one
The refrigerant of chemical constituent is planted, also including the mixed refrigerant systems of hydrocarbon precooling, and double-mixed refrigerant system.Generally, mix
Closing refrigerant includes hydrocarbon and/or non-hydrocarbon component.Be typically used for mix refrigerant suitable hydrocarbons component example can include but
It is not limited to methane, ethane, ethene, propane, propylene, butane and butylene isomer, and pentane.It is generally used in mix refrigerant
Non-hydrocarbon component can include nitrogen.Mixed refrigerant process uses at least one blending ingredients refrigerant, but can also volume
It is outer to use one or more pure component refrigerants.
" natural gas " refers to the multicomponent gas obtained by crude oil well or underground aerogenesis rock stratum.The composition and pressure of natural gas
Power can be with dramatically different.Typical natural gas stream includes methane (CH4) as key component, i.e., it is natural more than 50mol%
Gas logistics is methane.Natural gas stream can also include ethane (C2H6), hydrocarbon (such as C of higher molecular weight3-C20Hydrocarbon), Yi Zhonghuo
Various sour gas (such as carbon dioxide or hydrogen sulfide), or their any joint.Natural gas can also include a small amount of
Impurity, such as water, nitrogen, iron sulfide, wax, crude oil or their any joint.Filled during cooling treatment due to eliminating
When poisonous substance or the compound of solidification so that natural gas stream in for embodiment before substantially can be purifying.
Just as used in the present invention, " natural gas liquids " (NGL) refers to its component for example typically than methane weight
And the hydrocarbon mixture condensed from natural gas.Some examples of the hydrocarbon component of NGL logistics include ethane, propane, butane and penta
Alkane isomers, benzene, toluene and other aromatic compounds.
" nitrogen deliverying unit " or " NRU " refer to being configured to receive natural gas feed stream and preparing substantially pure product
Any system or device of product logistics, the net product logistics are, for example, to be adapted to the methane stream of sale and arrived including about 30%
99% N2Nitrogen stream.The example of NRU types include low temperature distillation, pressure-variable adsorption (PSA), UF membrane, Poor oil absorbing with
And solvent absorption.
" refrigerant component " in refrigeration system will at relatively low temperatures and pressures by evaporating absorption heat and inciting somebody to action
By condensing discharge heat under temperature and pressure higher.Illustrative refrigerant component can include but is not limited to have 1
To 5 alkane of carbon atom, alkene and alkynes, nitrogen, chlorohydrocarbon, fluorohydrocarbon, other halogenated hydrocarbons, inert gas and they
Mixture or joint.
Refrigerant component generally includes one-component refrigerant.One-component refrigerant with monohaloalkyl hydrocarbon has two or three
Correlation " R- " mark of individual numeral, its chemical composition for having reacted it.The numeral Jia 90 and to give that represent respectively carbon, hydrogen and fluorine former
Three numerals of subnumber purpose.First digit with three refrigerants of numeral is a list less than carbon number in molecule
Unit.If only containing a carbon atom in molecule, first digit is omitted.Second digit is more than number of hydrogen atoms in molecule
A unit.Third digit is equal to the number of fluorine atoms in molecule.Unaccounted remaining key is occupied by chlorine atom.Small letter
Female suffix " a ", " b " or " c " represents increased asymmetry isomer.Used as special situation, R-400 series is total to by non-azeotrope
Mixed thing is constituted, and R-500 series is made up of so-called azeotropic blend.Rightmost numeral by any assignment of ASHRAE, its
It is industrial organization.
When " substantial " amount or quantity or its special characteristic for referring to material, expression is enough to provide hope should
The quantity of the effect that material or characteristic are provided.The practical extent for deviateing can be allowed to depend in some cases special upper and lower
Text.
Summary of the invention
The embodiment of present invention description provides a kind of hydrocarbon system of processing.The hydrocarbon system of processing includes refrigeration system, example
Cooling system is such as cascaded, to prepare LNG by natural gas.The refrigeration system includes two fluorocarbons refrigeration systems and nitrogen
Or methane refrigeration systems associated.The fluorine carbon can also be used for cooled natural gas with without refrigeration system and nitrogen or methane refrigeration systems associated, so that
Prepare LNG.Additionally, the hydrocarbon system of processing can include NRU, it can be used for removing nitrogen from the LNG for preparing.
Hydrocarbon system of processing includes any number of system well known by persons skilled in the art.Prepared by hydrocarbon and processing procedure includes
But it is not limited to chilling natural gas to be extracted for NGL, for hydrocarbon dew point control, chilling natural gas is used to remove CO chilling natural gas2,
LPG production storages, the condensation flowed back in dethanizer/domethanizing column, and natural gas liquefaction is preparing LNG.
Although many kind of refrigeration cycle may be used to process hydrocarbon, a kind of circulation for LNG liquefaction plants is cascade cycle,
It is in the heat exchanger for arranging step by step using the refrigerant of multiple independent components to reduce the temperature of the gases to condensing temperature.
Another circulation for being used for LNG liquefaction engineerings is multiple group sub-refrigerating circulation, and it uses multicomponent in the exchanger of particular design
Refrigerant.Additionally, another circulation for LNG liquefaction engineerings is expander cycle, it makes the gas pressure from unstripped gas
It is expanded into relatively low pressure and the corresponding reduction with temperature.The change that NG Liquefaction cycle can also be circulated using these three
Shape or joint.
The LNG prepared by refrigeration and liquefaction technology by unstrpped gas.Optional step includes removing condensate, removes
CO2, dehydration, removing mercury, removing nitrogen, removing H2S and similar step.After liquefaction, LNG can store or be loaded into oil tanker
It is upper to be used to sell or transport.Conventional liquifying method includes：The hybrid refrigeration that APCI propane pre-coolings go；C3MR；DUAL MR；
Phillips optimizes cascade；Prico single mix refrigerant；The double pressure mix refrigerants of TEAL；Linde/Statoil is more
Fluid is cascaded；Axens double-mixed refrigerants；DMR；With Shell techniques C3MR and DMR.
Carbon dioxide is removed, will methane and light gas and CO2Separated with heavy gas, this can use low temperature distillation
Method is implemented, the controllable solidification area technology for for example being obtained by ExxonMobil Corporation.
Although the method and system of present invention description is on the discussion by natural gas adsorption LNG, described method and system
Can be also used for various other purposes.Such as method and system of the present invention can be used for chilling natural gas and reveal for hydrocarbon
Point control, carries out natural gas liquids (NGL) extraction, and methane and light gas are separated with carbon dioxide and heavy gas, makes
It is ready for use on the hydrocarbon of LPG productions, or condensing reflux logistics etc. in dethanizer and/or domethanizing column.
Refrigerant
Can be one or more one-component refrigerant for the refrigerant according to embodiment of the present invention, or
Including multi-component refrigerant mixture.Refrigerant can be with import or stored on-site, or alternatively, some components of refrigerant can
To prepare at the scene, it is typically prepared by the still-process integrated with hydrocarbon system of processing.Commercially available refrigerant bag
Fluorocarbons (FC) or HFC (HFC) are included, it can be used in various applications.Exemplary refrigerant can be by
DuPont Corporat ion are commercially available, includingSerial refrigerant,Serial refrigerant,Serial refrigerant, andSerial refrigerant.
Multi-component refrigrant is commercially available.For example, R-401A is the HCFC blends of R-32, R-152a and R-124.R-
404A is the HFC blends of the R-134a of the R-125 and 4wt.% of R-143a, 44wt.% of 52wt.%.R-406A is
The blend of the R-142b of the R-600a and 41wt.% of R-22,4wt.% of 55wt.%.R-407A be 20wt.% R-32,
The HFC blends of the R-134a of the R-125 and 40wt.% of 40wt.%.R-407C is the HFC of R-32, R-125 and R-134a
Compound blend.R-408A is the HCFC blends of R-22, R-125 and R-143a.R-409A is R-22, R-124 and R-
The HCFC blends of 142b.R-410A is the blend of R-32 and R-125.R-500 be 73.8wt.% R-12 and
The blend of the R-152a of 26.2wt.%.R-502 is the blend of R-22 and R-115.R-508B is being total to for R-23 and R-116
Mixed thing.
In different embodiments, what any number of different types of hydrocarbon system of processing can be described with the present invention appoints
What refrigeration system is used together.Additionally, the refrigeration system of present invention description can be any refrigerant using present invention description.
Refrigeration system
Hydrocarbon system and method generally include to use the refrigeration system of mechanical refrigeration, valve expansion, turbine expansion or similar techniques
System.Mechanical refrigeration is typically include compressibility and absorption system, such as aqua-ammonia absorption system.Compressibility is for various work works
Skill is used for gas processing industry.For example, compressibility can be used for chilling natural gas is used for hydrocarbon for NGL extractions, chilling natural gas
Dew point is controlled, LPG production storages, the condensation flowed back in dethanizer or domethanizing column, and natural gas liquefaction is preparing LNG or similar
Operation.
Fig. 1 is the process chart of single phase refrigeration system 100.In different embodiments, single phase refrigeration system
100 refrigerants for using such as fluorocarbons.Additionally, in different embodiments, single phase refrigeration system 100 is including
The nitrogen refrigeration or methane of NRU are implemented from the upstream of refrigeration system.Multiple single phase refrigeration systems 100 can also be in this nitrogen
Refrigeration system or methane are implemented from refrigeration system upstream tandem.
Single phase refrigeration system 100 includes expansion valve 102, quencher 104, compressor 106, condenser 108 and material storage container
110.Saturated liquid refrigerant 112 can flow to expansion valve 102 from material storage container 110, and isenthalpic expansion passes through expansion valve 102.
There are some evaporations during expansion, generation includes the refrigerant mixture 114 of the chilling of steam and liquid.Refrigerant mixture 114
Quencher 104 can be entered at a temperature of being cooled to less than process-stream 116, such as natural gas, the quencher it is known that
As evaporator.Process-stream 116 flows through quencher 104 and is exchanged heat with coolant mixture 114.With process-stream 116
Exchanged heat with coolant mixture 114, process-stream 116 is cooled down, and refrigerant mixture 114 evaporates, produced the steaming of saturation
Gas refrigerant 118.
Leave after quencher 104, the vaporous cryogen 118 of saturation is compressed in compressor 106, and flows to afterwards cold
Condenser 108.In condenser 108, the vaporous cryogen 118 of saturation changes into liquid refrigerant saturation or being slightly subcooled
120.Material storage container 110 can be flowed to after liquid refrigerant 120 from condenser 108.The material storage container 110 is also known as surge tank
Or receiver, can serve as the holder for liquid refrigerant 120.Liquid refrigerant 120 expand through expansion valve 102 it
Before can be stored in material storage container 110 as saturated liquid refrigerant 112.
It should be understood that the process chart of Fig. 1 is not intended to illustrate that single phase refrigeration system 100 includes what Fig. 1 showed
All constituents.Additionally, single phase refrigeration system 100 can include the not shown any number of other components of Fig. 1,
This depends on the details of particular embodiment.For example, in some embodiments, refrigeration system can include two or more
Compression stage.Additionally, refrigeration system 100 may include to save device, as related Fig. 2 is discussed further.
Fig. 2 is the process chart for including the two benches refrigeration system 200 for saving device 202.Similar numeric item according to
Fig. 1 related project is described.In different embodiments, two benches refrigeration system 200 uses such as fluorocarbons
Refrigerant.Additionally, in different embodiments, two benches refrigeration system 200 the nitrogen including NRU freeze or methane from
Implement the upstream of refrigeration system.Multiple two benches refrigeration systems 200 can also certainly freeze in this nitrogen refrigeration system or methane
The upstream tandem of system is implemented.
It can be that any device or method for reducing the compressor horsepower for giving quencher load change to save device 202
Enter.Conventional saving device 202 for example includes that flash tank and heat exchanger save device.Plus heat exchanger uses multiple in process-stream
Between transmit heat heat exchanger.This can by by process-stream each other heat integration and reduce and be input to two benches refrigeration system
The amount of the energy in 200.
As shown in Fig. 2 the saturated liquid refrigerant 112 for leaving material storage container 110 can be expanded through during expansion valve 102 reaches
Deng pressure, steam and liquid can be separated at this pressure.For example, as saturated liquid refrigerant 112 is flashed through expansion valve
102, it is prepared for vaporous cryogen 204 and liquid refrigerant under the pressure and temperature lower than saturated liquid refrigerant 112
206.Then vaporous cryogen 204 and liquid refrigerant 206 can flow into saving device 202 in.In different embodiments,
It is to carry out the flash tank that vaporous cryogen 204 and liquid refrigerant 206 are separate to save device 202.Vaporous cryogen 204 can flow
To middle pressure compressor stage, vaporous cryogen 204 can be with the saturated vapor left from the first compressor 210 there
Refrigerant 118 merges, and generates the saturated vapor refrigerant 208 of mixing.Can be flowed to after the saturated vapor refrigerant 208 of mixing
Second compressor 212.
Second expansion valve 214 can be passed through with isenthalpic expansion from the liquid refrigerant 206 for saving device 202.Meeting during expansion
There are some evaporations, generation includes the refrigerant mixture 216 of steam and liquid, so as to reduce temperature and pressure.Refrigerant
Mixture 216 will have than without the content liquid higher of the refrigerant mixture in the system for saving device.Liquid higher
Content can reduce refrigerant circulation speed and/or reduce the energy ezpenditure of the first compressor 210.
Refrigerant mixture 216 at a temperature of less than the temperature to be cooled to of process-stream 116 enter be also known as
In the quencher 104 of evaporator.As being discussed in related Fig. 1, the process-stream 116 is cooled down in quencher 104.
Additionally, the vaporous cryogen 118 of saturation flows through compressor 210 and 212 and condenser 108, and the liquid refrigerant for producing
120 are stored in material storage container 110, as being discussed in related Fig. 1.
It is appreciated that the process chart of Fig. 2 is not intended to explanation two benches refrigeration system 200 to include being shown in Fig. 2
All constituents.Additionally, two benches refrigeration system 200 can include not shown any number of other composition portions of Fig. 2
Point, this depends on the details of particular embodiment.For example, two benches refrigeration system 200 can be including not shown any in Fig. 2
Other of number save device or other kinds of equipment.Additionally, save device 202 can be heat exchanger save device rather than
Flash tank.Heat exchanger saves device and can be also used for reducing kind of refrigeration cycle speed and reducing compressor energy ezpenditure.
In some embodiments, two benches refrigeration system 200 includes more than one saving device 202, and is more than
The compressor 210 and 212 of two.For example, two benches refrigeration system 200 can include two saves device and three compressors.
Generally, if refrigeration system 200 includes X saving device, then the refrigeration system 200 will be including X+1 compressor.This tool
Having multiple refrigeration systems 200 for saving device can form a part for cascade refrigeration system.
Fig. 3 is to include that heat exchanger saves the process chart of the single phase refrigeration system 300 of device 302.Similar numeric item
It is described according to the project related to Fig. 1.In different embodiments, single phase refrigeration system 300 uses such as fluorine carbon
The refrigerant of compound.Additionally, in different embodiments, single phase refrigeration system 300 freeze in the nitrogen including NRU or
Methane is implemented from the upstream of refrigeration system.Multiple single phase refrigeration systems 300 can also be in this nitrogen refrigeration system or methane
Implement from the upstream tandem of refrigeration system.
As shown in figure 3, the saturated liquid refrigerant 112 for leaving material storage container 110 can be expanded through during expansion valve 102 reaches
Deng pressure, steam and liquid can be separated and prepare refrigerant mixture 114 at this pressure.The refrigerant mixture 114 can be with
Quencher 104 is flowed under the temperature lower temperature than cooling technique logistics 116.The process-stream 116 can be in quencher
Cooled down in 104, as related Fig. 1 is discussed.
Saturated vapor refrigerant 118 from quencher 104 can flow through heat exchanger and save device 302.Cold, low pressure is satisfied
The saturated liquid refrigerant 112 in heat exchanger saving device 302 is may be used to vaporous cryogen 118 to be subcooled.From heat exchanger
Save and can flow through after the superheated vapor refrigerant 304 out of device 302 compressor 106 and condenser 108, and obtain
Liquid refrigerant 120 can be stored in material storage container 110, as related Fig. 1 is discussed.
It is appreciated that the process chart of Fig. 3 is not intended to explanation single phase refrigeration system 300 to include being shown in Fig. 3
All constituents.Additionally, single phase refrigeration system 300 can include not shown any number of other composition portions of Fig. 3
Point, this depends on the details of particular embodiment.
Fig. 4 is the technological process of the cascade cooling system 400 for including the first refrigeration system 402 and the second refrigeration system 404
Figure.In different embodiments, the first refrigeration system 402 and the second refrigeration system 404 have used fluorocarbons refrigerant.
For example, the first refrigeration system 402 can use R-410A, and the second refrigeration system 404 can use R-508B.Additionally, in system
Refrigerant in cooling system 402 or 404 can include mixture.Cascade cooling system 400 for example can be used for than expecting to freeze
The cooling of the higher degree that system 100,200 or 300 can be provided.Cascade cooling system 400 can be provided under very low temperature
Cooling, such as less than -40 DEG C.Additionally, in some embodiments, cascade cooling system 400 is in nitrogen refrigeration system or methane
Implement from the upstream of refrigeration system.
In the first refrigeration system 402, vapor/liquid refrigerant stream 406 can flow through first from material storage container 408
Expansion valve 410 and First Heat Exchanger 412, its chilling product stream 413.The steam stream for obtaining divides in the first flash tank 414
From.A part of vapor/liquid cooling agent logistics 406 can be flowed directly at the first flash tank 414 by bypass valve 416.
Liquid refrigerant logistics 418 from flash tank 414 can flow through the second expansion valve 420, and flash and enter
Two heat exchangers 422, it can be used for further chilling product stream 413.The vaporous cryogen thing that gas material storage container 424 will be obtained
Stream 426 is fed at first stage compressor 428.The middle pressure vaporous cryogen logistics 430 that obtains with from flash tank 414
Vaporous cryogen logistics 432 merge, and the logistics of merging is fed at second stage compressor 434.From second-order
The HCS logistics 436 of section compressor 434 passes through condenser 438, and it can be used from the cold of the second refrigeration system 404
But.Particularly, condenser 438 can use the low-temperature refrigerant logistics 440 from the second refrigeration system 404 to cool down HCS
Logistics 436 is preparing liquid refrigerant logistics 406.It is stored in after liquid refrigerant logistics 406 from refrigeration condenser 438
In material pond 408.Control valve 442 can be used for controlling low-temperature refrigerant logistics 440 through the flowing of condenser 438.To make by oneself
The vaporous cryogen logistics 444 for obtaining of condenser 438 can flow back into the second refrigeration system 404.
In the second refrigeration system 404, liquid refrigerant logistics 448 can flow through from material storage container 450 and be configured to pass urgency
Cooling system 454 makes the heat exchanger 452 that liquid refrigerant logistics 448 is cooled down.The chilling system 454 for example can be from different technique
Logistics is exchanged heat, for example, come since the natural gas stream of the final flash tank that NGL is separated in gas.
The low-temperature refrigerant logistics 456 for obtaining can flow through the first expansion valve 458 and First Heat Exchanger 460, and its chilling is produced
Product logistics 413.The vapor/liquid refrigerant stream for obtaining is separated in the first flash tank 462.A part of low-temperature refrigerant logistics
456 can flow directly into the first flash tank 462 by bypass valve 464, and the valve can be for controlling fluid to enter flash distillation
The Level control valve of groove 462.
Liquid refrigerant logistics 466 from the first flash tank 462 can flow through the second expansion valve 468, and flash into
Enter the second heat exchanger 470, it can be used for further chilling product stream 413.The vapor/liquid refrigerant stream for obtaining can be with
Separated in the second flash tank 472.A part of liquid refrigerant logistics 466 can flow directly into second by bypass valve 474
Flash tank 472, the valve can be used for controlling the fluid temperature in the second flash tank 472, and cold in the second heat exchanger 470
But measure.
Liquid refrigerant logistics 476 from the second flash tank 472 can flow through the 3rd expansion valve 478, and flash into
Enter the 3rd heat exchanger 480, it can be used for further chilling product stream 413.The steam refrigerating that gas material storage container 482 will be obtained
Agent logistics 484 is fed in first stage compressor 486.The middle pressure vaporous cryogen logistics 488 that obtains with from second
The vaporous cryogen logistics 490 of flash tank 472 merges, and the logistics of merging is fed in second stage compressor 492.
To HCS refrigerant stream 494 merge with the vapor refrigerant mixture 496 from the first flash tank 462, and will
The logistics of merging is fed in phase III compressor 497.The HCS refrigerant stream 498 for obtaining flows through heat exchanger 499,
Wherein it further can be cooled down by with cooling water indirect heat exchange.Can after the liquid refrigerant logistics 448 for obtaining
To flow to material storage container 450.
It should be understood that the process chart of Fig. 4 is not intended to explanation cascade cooling system 400 includes the institute that Fig. 4 shows
There is part.Additionally, cascade cooling system 400 can include the not shown any number of other components of Fig. 4, this takes
Certainly in the details of particular embodiment.
Fig. 5 is the process chart of the expansion refrigeration system 500 for hydrocarbon dew point control.The weight in natural gas in pipeline
Matter hydrocarbon, such as C3-C6The condensation of heavy hydrocarbon impact and gas of the liquid in pipeline can be caused to receive the rupture of facility.Cause
This, hydrocarbon dew point can be reduced using expansion refrigeration system 500, to prevent this condensation.
As shown in figure 5, the natural gas material stream 502 of dehydration can be with inflow gas/gas heat exchanger 504.In gas/gas
In body heat exchanger 504, the natural gas material stream 502 of dehydration can be cold by the indirect heat exchange with cryogenic natural gas logistics 506
But.The natural gas stream 508 for obtaining can be flowed into the first separator 510, and it can remove same amount of from natural gas thing
The heavy hydrocarbon 512 of stream 508.In different embodiments, remove the heavy hydrocarbon 512 from natural gas stream 508 and reduce day
The dew point of right gas logistics 508.The heavy hydrocarbon 512 of removing can flow out expansion refrigeration system 500 by first outlet valve 514.
For example, heavy hydrocarbon 512 can flow to stabilizer (not shown) from expanding refrigerant system 500.
During natural gas stream 508 can flow into expander 516 afterwards.In different embodiments, expander 516 is
Flat expander, it is centrifugation or axial turbine.The expansion of natural gas stream 508 can provide energy and be used in expander 516
Compressor 518 is driven, it is connected with expander 516 by axostylus axostyle 520.
The cryogenic natural gas logistics 506 for obtaining for carrying out expander 516 can flow to the second separator 522, and it can be from
The heavy hydrocarbon 512 of any residual is removed in cryogenic natural gas logistics 506.In different embodiments, from cryogenic natural gas thing
The dew point that heavy hydrocarbon 512 reduce further cryogenic natural gas logistics 506 is removed in stream 506.Then the heavy hydrocarbon 512 for removing can
Expansion refrigeration system 500 is flowed out with by second outlet valve 524.
Cryogenic natural gas logistics 506 can flow to gas/gas heat exchanger 504 from the second separator 522, and it can make low
The temperature of warm natural gas stream 506 is raised, so as to prepare high-temperature natural gas logistics 526.Can be with after high-temperature natural gas logistics 526
Compressor 518 is flowed through, it can make the pressure of natural gas stream 526 return to acceptable sales gas pressure.Finally, dew is reduced
Expansion refrigeration system 500 can be flowed out after the natural gas stream 528 of point.
In one embodiment, can for example be used using the cooling system of fluorocarbons refrigerant and nitrogen gas refrigerant
In further cooling of the increase to process.This cooling can be in natural gas stream 508 or low by the way that heat exchanger 530 is placed on
In warm natural gas stream 506, implement in the upstream of the second separator 522.Refrigerant liquid 532 can be flashed through expansion valve
534, by quencher 530.The refrigerant vapour 536 for obtaining may return in refrigeration system afterwards.The chilling can allow to remove
Remove the condensable hydrocarbon of higher amount, such as C3And higher hydrocarbon.Additionally, in some embodiments, heat exchanger 530 is placed on expansion
The upstream of device 516, it has the separator between heat exchanger 530 and expander 516 to prevent liquid flow to expander
516。
It is appreciated that the process chart of Fig. 5 is not intended to illustrate that expansion refrigeration system 500 includes the institute that Fig. 5 shows
There is part.Additionally, expansion refrigeration system 500 can include the not shown any number of other components of Fig. 5, this takes
Certainly in the details of particular embodiment.For example, in some embodiments, expansion refrigeration system 500 is including two fluorine carbonizations
The implementation in the cascade cooling system of nitrogen refrigeration system upstream of compound refrigeration system.In these embodiments, flash
It is the fluorine carbon from one of fluorocarbons refrigeration system through expansion valve 534 and the refrigerant liquid 532 for flowing through quencher 530
Compound refrigerant or the nitrogen gas refrigerant from nitrogen refrigeration system.
Fig. 6 is the process chart of the expansion cooling system 600 prepared for NGL.NGL extractions can be carried out to reclaim
NGL, it includes any number of different heavy hydrocarbons from natural gas stream.NGL extractions are desirable, because NGL is usual
Be more valuable purpose not as gas-phase heating fuel the fact.
Dry natural gas material stream 602 can from dewatering system inflow gas/gas heat exchanger 604.In gas/gas
In body heat exchanger 604, dry natural gas material stream 602 can be cooled down by the indirect heat exchange with cryogenic natural gas logistics 606.
The natural gas stream 608 for obtaining can be flowed into separator 610, and it can remove part NGL from natural gas stream 608
612.The NGL 612 of removing can flow to dethanizer or domethanizing column 614 from separator 610.
Natural gas stream 608 can be flowed into expander 616 afterwards.In different embodiments, expander 616 is
Flat expander.Natural gas stream 608 in expander 616 can be to drive compressor 618 to provide energy, and it passes through axostylus axostyle 620
It is coupled with expander 616.Additionally, the temperature of natural gas stream 608 can be carried out absolutely by through Joule-Thomson valve 622
Thermal expansion and reduce.
The cryogenic natural gas logistics 606 for obtaining for carrying out expander 616 can flow into dethanizer or domethanizing column 614
In.In dethanizer or domethanizing column 614, NGL can be separated from natural gas stream 606 and can be as NGL products
Logistics 624 flows out dethanizer or domethanizing column 614.Swell refrigeration can be pumped out by pump 626 after NGL product streams 624
System 600.
Dethanizer or domethanizing column 614 can be connected with heat exchanger 628.In some embodiments, heat exchanger 628 is
Reboiler 628, it can be used to heat a part from dethanizer or piptonychia by the indirect heat exchange in high temperature fluid 632
The bottoms 630 of alkane tower 614.Then the bottoms 630 for heating can be re-injected into dethanizer or domethanizing column 614
In.
Carried out in dethanizer or domethanizing column 614 separate NGL product streams 624 from natural gas stream 606 can
To cause the preparation of cryogenic natural gas logistics, the logistics can flow out dethanizer or domethanizing column as overhead stream 634
614.Overhead stream 634 can with inflow heat exchanger 636, the heat exchanger can by with refrigerant 638, such as fluorocarbons
The indirect heat exchange of refrigerant or nitrogen gas refrigerant and reduce the temperature of overhead stream 634.The reduction of temperature can cause some to steam
The condensation of gas.Then overhead stream 634 can separate to prepare cryogenic natural gas logistics 606 and liquid in separation container 640
Bottoms 642.During bottoms 642 can be pumped back to dethanizer or domethanizing column 614 by pump 644, recycling is formed
Logistics.
Cryogenic natural gas logistics afterwards 606 can flow through gas/gas heat exchanger 604.The temperature of cryogenic natural gas logistics 506
Degree can be raised in gas/gas heat exchanger 604, prepare high-temperature natural gas logistics 646.High-temperature natural gas logistics 646
Compressor 618 can be flowed through afterwards, its pressure that can increase natural gas stream 646.In some embodiments, high temperature is natural
Gas logistics 646 also flows through the second compressor 648, and the pressure of natural gas stream 646 can be increased to acceptable sales gas by it
Pressure.Then gas product logistics 650 can flow out expansion refrigeration system 600.
It is appreciated that the process chart of Fig. 6 is not intended to illustrate that expansion refrigeration system 600 includes the institute that Fig. 6 shows
There is part.Additionally, expansion refrigeration system 600 can include the not shown any number of other components of Fig. 6, this takes
Certainly in the details of particular embodiment.For example, in some embodiments, expansion refrigeration system 600 is including two fluorine carbonizations
Compound refrigeration system is implemented in being located at the cascade cooling system of nitrogen refrigeration system upstream.In these embodiments, in heat exchange
The refrigerant 638 used in device 636 is fluorocarbons refrigerant from one of fluorocarbons refrigeration system or from nitrogen
The nitrogen gas refrigerant of gas refrigeration system.
Fig. 7 is the process chart of LNG preparation systems 700.As shown in fig. 7, LNG 702 can use multiple different systems
Cooling system is prepared by natural gas stream 704.As shown in fig. 7, a part of natural gas stream 704 can enter LNG preparation systems
Separated from natural gas stream 704 before 700, and can serve as fuel gas stream 706.Remaining natural gas stream
During 704 can flow into initial gas processing system 708.In gas processing system 708, natural gas stream 704 can be with pure
Change and cool down.For example, natural gas stream 704 can be freezed using the first fluorocarbons refrigerant 710, the second fluorocarbons
Agent 712 and high pressure nitrogen refrigerant 714 are cooled down.The cooling of natural gas stream 704 can cause the preparation of LNG 702.
In LNG preparation systems 700, heavy hydrocarbon 716 can be removed from natural gas stream 704, and a part of heavy
Hydrocarbon 716 can be used for the gasoline 718 that preparation is prepared in heavy hydrocarbon system of processing 720.Additionally, from weight during the preparation of gasoline 718
The natural gas 722 of any residual in matter hydrocarbon 716 separate may return in natural gas stream 704.
The LNG 702 of preparation can include same amount of nitrogen 724.Therefore, LNG 702 can flow through NRU 726.NRU
726 isolate nitrogen 724 from LNG 702, prepare final LNG product.
It is appreciated that the process chart of Fig. 7 is not intended to illustrate that LNG preparation systems 700 include the institute that Fig. 7 shows
There is part.Additionally, LNG preparation systems 700 can include the not shown any number of other components of Fig. 7 or process
In for fluorocarbons refrigerant quencher diverse location, this depend on particular embodiment details.For example, any number
Purpose substitutes refrigeration system and can be also used for preparing LNG 702 from natural gas stream 704.Additionally, any number of different system
Cooling system can be combined with using preparing LNG 702.
For system prepared by LNG
Fig. 8 A and 8B are the process charts for cascading cooling system 800.The cascade cooling system 800 can be used for LNG's
Prepare, and can implement in hydrocarbon system of processing.The cascade cooling system 800 can be operated at low temperature, such as less than greatly
About -18 DEG C, or less than about -29 DEG C, or less than about -40 DEG C.Additionally, the cascade cooling system 800 can use it is many
Refrigeration is provided in a kind of refrigerant and at multiple temperature.
Cascade cooling system 800 can include the first fluorocarbons refrigeration system 802, and as shown in Figure 8 A, it can make
With the first fluorocarbons refrigerant, such as R-410A.Cascade cooling system 800 can also freeze including the second fluorocarbons
System 804, as shown in Figure 8 B, it can use the second fluorocarbons refrigerant, such as R-508B.Additionally, cascade cooling system
System 800 can include nitrogen refrigeration system 806, as shown in Figure 8 B.
Natural gas stream 808 can flow through quencher 810, and it is precooled naturally by the indirect heat exchange with cooling fluid
Gas logistics 808.Natural gas stream 808 can be flowed into the pipe joint 812 of cascade cooling system 800 afterwards.The pipe joint
812 are configurable to for natural gas stream 808 to be divided into three single natural gas streams.First natural gas stream can be by pipe
Line 814 is flowed into the first fluorocarbons refrigeration system 802, and the second natural gas stream and the 3rd natural gas stream can pass through
Pipeline 816 and 818 is separately flowed into the system with Fig. 9 relevant discussions.
Natural gas stream is used for cooled natural gas thing during the first fluorocarbons refrigeration system 802 can be flowed into preparation
Stream.The natural gas stream can be by through a series of heat exchangers 820 in the first fluorocarbons refrigeration system 802,822 and
824 are cooled down.The heat exchanger 820,822 and 824 may also refer to evaporator, quencher or ice chest.Natural gas stream can
It is cold to be carried out in each by the indirect heat exchange with circulation fluorocarbons refrigerant in heat exchanger 820,822 and 824
But.The fluorocarbons refrigerant can be HFC, such as R-410A or R-404A, or any other is suitable
The fluorocarbons refrigerant of type.
Fluorocarbons refrigerant can be circulated continuously through the first fluorocarbons refrigeration system 802, and it can be even
Continuous prepares fluorocarbons refrigerant to enter each in heat exchanger 820,822 and 824.Fluorocarbons refrigerant
Steam fluorocarbons refrigerant can be used as by pipeline 826 and flow out First Heat Exchanger 820.Steam fluorocarbons refrigerant
Can merge in two pipe joints 828 and 829 with other steam fluorocarbons refrigerants.Then vapor stream overcompression machine
830, to increase the pressure of steam fluorocarbons refrigerant, prepare the steam fluorocarbons refrigerant of overheat.The steam of overheat
Fluorocarbons cold-producing medium stream crosses condenser 832, and it can cool down and condense superheated vapor fluorocarbons refrigerant, prepares
Liquid fluorocarbon compound refrigerant.
Liquid fluorocarbon compound refrigerant can flow through expansion valve 834, which reduce liquid fluorocarbon compound refrigerant
Temperature and pressure.This can cause the flash distillation of liquid fluorocarbon compound refrigerant, prepare liquid fluorocarbons refrigerant and steaming
The mixture of gas fluorocarbons refrigerant.Liquid fluorocarbon refrigerant and steam fluorocarbons refrigerant can be by pipelines
838 flow into the first flash tank 836.In the first flash tank 836, liquid fluorocarbon compound refrigerant can be from steam fluorine carbon compound
Separated in thing refrigerant.
Steam fluorocarbons refrigerant can be flowed at pipe joint 828 by pipeline 839 from the first flash tank 836.
The liquid fluorocarbon compound refrigerant can be so that in inflow line joint 840, can be divided into for liquid fluorocarbon compound refrigerant by it
Two single liquid fluorocarbon compound refrigerant streams.One liquid fluorocarbon compound refrigerant stream can flow through first and change
Hot device 820, partly or entirely flashes to steam, and return at pipe joint 828 by pipeline 826.Other liquid fluorines are carbonized
Compound refrigerant stream can be flowed at the second flash tank 842 by pipeline 844.Pipeline 844 also includes expansion valve 846, and it can
Liquid fluorocarbon compound refrigerant stream is controlled to enter the second flash tank 842 to adjust liquid fluorocarbon compound refrigerant stream
Flowing.The regulation of liquid fluorocarbon compound refrigerant stream can cause liquid fluorocarbon compound to freeze in expansion valve 846
The flash vaporization of agent logistics, so as to prepare the mixture of both steam and liquid fluorocarbon compound refrigerant.
Second flash tank 842 can separate liquid fluorocarbon compound refrigerant with steam fluorocarbons refrigerant.Should
Steam fluorocarbons refrigerant can be by the inflow line joint 848 of pipeline 850.The pipe joint 848 can merge steaming
Gas fluorocarbons refrigerant and the steam fluorocarbons refrigerant reclaimed from the second heat exchanger 822.The steam fluorine is carbonized
In can flowing into another pipe joint 852 after compound refrigerant.The pipe joint 852 can merge steam fluorocarbons
Refrigerant and the steam fluorocarbons refrigerant reclaimed from the 3rd heat exchanger 824.The steam fluorocarbons refrigeration of merging
Agent can pressurize and by the inflow line joint 829 of pipeline 856 in compressor 854 to merge from the He of flash tank 836
The steam of heat exchanger 820.
Liquid fluorocarbon compound refrigerant can be flowed at pipe joint 858 from the second flash tank 842, and it can be by liquid
Fluorocarbons refrigerant is divided into two single liquid fluorocarbon compound refrigerant streams.One liquid fluorocarbon compound refrigeration
Agent logistics can flow through the second heat exchanger 822 and be returned at pipe joint 848 by pipeline 860.Another liquid fluorine is carbonized
Compound refrigerant stream can flow through the 3rd heat exchanger 824 by pipeline 862.Pipeline 862 can also include expansion valve 864, should
Expansion valve allows liquid fluorocarbon compound refrigerant stream to flash, and thus reduces liquid fluorocarbon compound refrigerant stream
Pressure and temperature, when it flows into three heat exchangers 824.Liquid fluorocarbon compound refrigerant thing from the 3rd heat exchanger 824
Stream can be compressed in compressor 866 and is sent at pipe joint 852 by pipeline 868.
In different embodiments, the fluorocarbons refrigerant of the second fluorocarbons refrigeration system 804 is first
Precooled in fluorocarbons refrigeration system 802.For example, the fluorocarbons refrigerant of the second fluorocarbons refrigerant can be with
It is pre-cooled by flowing through First Heat Exchanger 820.The fluorocarbons refrigerant can be HFC, such as R-
508B, or any other suitable type fluorocarbons.The fluorocarbons refrigerant can be by pipeline 870 from
Two fluorocarbons refrigeration systems 804 flow to First Heat Exchanger 820.
In each of natural gas stream in heat exchanger 820,822 and 824 gradually after chilling, it just passes through pipeline 874
In flowing into the second fluorocarbons refrigeration system 804, as shown in Figure 8 B.Second fluorocarbons refrigeration system 804 can include
4th heat exchanger 876 and the 5th heat exchanger 878, it can use the further cooled natural gas logistics of fluorocarbons refrigerant.
Fluorocarbons refrigerant can be continuously circulated through the second refrigeration system 804, and it prepares fluorocarbons refrigeration
Agent is used to enter each in heat exchanger 876 and 878.The fluorocarbons refrigerant can be as steam fluorocarbons system
Refrigerant stream from the 4th heat exchanger 876 out.The steam fluorocarbons refrigerant stream can be with another steam fluorine carbon
Compound refrigerant stream merges in pipe joint 880, and also can be with another steam from the 5th heat exchanger 878
Fluorocarbons refrigerant stream merges in another pipe joint 882.Then the steam fluorocarbons refrigerant stream
Compressor 884 can be flowed through, it can increase the pressure of steam fluorocarbons refrigerant stream, prepare the fluorine carbonization of overheat
Compound refrigerant stream.The fluorocarbons refrigerant stream of overheat can flow through pipe joint 886 and another compressor
888, its pressure that can further increase overheat fluorocarbons refrigerant stream.
Overheat fluorocarbons refrigerant stream can flow through gas cooler 890.The gas cooler 890 can be cooled down
Overheat fluorocarbons refrigerant stream, prepares the steam fluorocarbons refrigerant stream of cooling.In some cases, if
Steam fluorocarbons refrigerant stream is less than environment temperature, and the steam fluorocarbons refrigerant stream can't be flowed through
Gas cooler 890.The first fluorocarbons system can be flowed through by pipeline 870 after liquid fluorocarbon compound refrigerant stream
First Heat Exchanger 820 in cooling system 802.
Once fluorocarbons refrigerant stream passes through First Heat Exchanger 820, the fluorocarbons refrigerant stream can lead to
Cross the 3rd flash tank 892 that pipeline 894 enters in the second fluorocarbons refrigeration system 804.Pipeline 894 can include control fluorine
Carbon compound refrigerant stream flows into the expansion valve 896 of the 3rd flash tank 892.The expansion valve 896 can reduce fluorocarbons
The temperature and pressure of refrigerant stream, this causes the flash vaporization of fluorocarbons refrigerant stream to be freezed for steam fluorocarbons
Both agent logistics and liquid fluorocarbon compound refrigerant stream.
Steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream can be flashed into the 3rd sudden strain of a muscle
Steam in groove 892, it can separate steam fluorocarbons refrigerant stream with liquid fluorocarbon compound refrigerant stream.The steaming
Gas fluorocarbons refrigerant stream can be by the inflow line joint 886 of pipeline 898.Liquid fluorocarbon compound refrigerant stream
4th flash tank 904 can be flowed into from the 3rd flash tank 892 by pipeline 906.Pipeline 906 can include control fluorocarbons
Refrigerant stream flows into the expansion valve 908 of the 4th flash tank 904.The expansion valve 908 can further reduce fluorocarbons system
The temperature and pressure of refrigerant stream, this causes the flash vaporization of fluorocarbons refrigerant stream to be steam fluorocarbons refrigerant
Both logistics and liquid fluorocarbon compound refrigerant stream.
Liquid fluorocarbon compound refrigerant stream can be left at pipe joint 910 from the 4th flash tank 904, and it can be by
Liquid fluorocarbon compound refrigerant stream is divided into two single liquid fluorocarbon compound refrigerant streams.One liquid fluorine carbonization
Compound refrigerant stream can flow through the 4th heat exchanger 876 and by the return line joint 880 of pipeline 912 at.Another liquid
Body fluorocarbons refrigerant stream can flow through the 5th heat exchanger 878 by pipeline 914.Pipeline 914 can also include control
Liquid fluorocarbon compound refrigerant stream flows into the expansion valve 916 of the 5th heat exchanger 878, for example, by allowing fluorocarbons
Refrigerant stream is flashed, and is reduced temperature and is produced steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant
Logistics.The steam fluorocarbons refrigerant stream for obtaining from the 5th heat exchanger 878 can pressurize simultaneously in compressor 918
And afterwards in inflow line joint 882 to recycle.
Natural gas stream is cold by the indirect heat exchange with fluorocarbons refrigerant stream in heat exchanger 876 and 878
But after, natural gas stream can flow into nitrogen refrigeration system 806 by pipeline 920.In different embodiments, nitrogen system
The nitrogen gas refrigerant logistics of cooling system 806 by flow through each in heat exchanger 820,822,824 and 876 carry out precooling.Nitrogen
Gas refrigerant stream can flow to heat exchanger 820,822,824 and 876 by pipeline 921 from nitrogen refrigeration system 806.
In nitrogen refrigeration system 806, natural gas stream can in the 6th heat exchanger 922 by with nitrogen gas refrigerant thing
The indirect heat exchange of stream and cool down.Nitrogen gas refrigerant logistics can continuously cycle through nitrogen refrigeration system 806, and it is prepared for using
In the nitrogen gas refrigerant logistics for entering the 6th heat exchanger 922.Nitrogen gas refrigerant can be as two single nitrogen gas refrigerant things
Stream flows through the 6th heat exchanger 922.Nitrogen gas refrigerant logistics from the 6th heat exchanger 922 can merge in pipe joint 924.
The nitrogen gas refrigerant logistics of merging can flow through the 7th heat exchanger 926 by pipeline 928.In the 7th heat exchanger 926
In, nitrogen gas refrigerant logistics can provide cooling to the high pressure nitrogen refrigerant stream for flowing in the opposite direction.Changed from the 7th
The nitrogen gas refrigerant logistics of hot device 926 can pressurize in the first compressor 930, be cooled down in the first quencher 932, second
Pressurizeed in compressor 934, and cooled down in the second quencher 936.Can be flowed after the high pressure nitrogen refrigerant stream for obtaining
Enter pipe joint 938, high pressure nitrogen refrigerant stream can be divided into two single high pressure nitrogen refrigerant streams by it.
A high pressure nitrogen refrigerant stream from pipe joint 938 can by pipeline 921 flow through heat exchanger 820,
822nd, 824 and 876.Once leaving the 4th heat exchanger 876, nitrogen gas refrigerant logistics can be expanded in expander 940 so as to produce
Raw energy, and the 6th heat exchanger 922 is flowed through to provide the cooling to natural gas stream.
Another high pressure nitrogen refrigerant stream can flow through the 3rd compressor 942, the 3rd quencher from pipe joint 938
944 and the 7th heat exchanger 926.Can be expanded in expander 946 so as to produce energy after high pressure nitrogen refrigerant stream, and
And the 6th heat exchanger 922 is flowed through to provide cooling for natural gas stream.The energy produced in expander 940 and 946
For generating electricity or driving all or some (part) in compressor 930,934 or 942.
Fig. 9 is the process chart for including the system 900 of NRU 902.The system 900 may be located at cascade cooling system
800 downstream, and can implement in the cascade identical hydrocarbon system of processing of cooling system 800.
Once natural gas stream is cooled down in nitrogen refrigeration system 806, the natural gas stream can be just the form of LNG.
The LNG stream can flow into system 900 by pipeline 948.Particularly, the LNG stream can be with inflow line joint 950, and it can
To merge the LNG stream from pipeline 948 and the natural gas stream from pipeline 816.Natural gas stream from pipeline 816
Initial cooling can be carried out before natural gas stream inflow line joint 950 in the 8th heat exchanger 952.
LNG stream from pipe joint 950 can be flowed into NRU 902 to remove excessive nitrogen from LNG stream
Gas.Particularly, the LNG stream can flow into reboiler 954, its temperature that can reduce LNG stream.The LNG stream of cooling can
With in hydraulic expansion turbine 956 expand and flow through expansion valve 958 afterwards, which reduce the temperature and pressure of LNG stream
Power.
LNG stream can flow into the low-temperature fractionation post 960 in NRU902, such as NRU towers.Furthermore, it is possible to pass through pipeline 962
Heat is delivered to low-temperature fractionation post 960 from reboiler 954.Low-temperature fractionation post 960 can by cryogenic distillation process by nitrogen from
Separated in LNG stream.Overhead stream can flow out low-temperature fractionation post 960 by pipeline 964.Overhead stream can be wrapped mainly
Include methane, nitrogen and other low boilings or uncondensable gas, such as helium, it is separated from LNG systems.
In some embodiments, during overhead stream flows into evaporator overhead condenser (not shown), it can be in overhead stream
In separating any liquid and it is returned to low-temperature fractionation post 960 as backflow.This can cause a kind of steam stream, main bag
Include the preparation of the fuel stream and the main another steam stream including low-boiling point gas of methane.Fuel stream can be by pipe
Line 964 flows through the 8th heat exchanger 952.In the 8th heat exchanger 952, the temperature of vapor fueled logistics can by with natural gas thing
The indirect heat exchange of stream and raise, produce vapor fueled logistics.The vapor fueled logistics can be with other vapor fueled logistics in pipe
Merge in wire terminal 966.Can be in a series of compressors 968,970 and 972 and chilling after the vapor fueled logistics for merging
Cooled down in device 974,976,978.In pipe joint 980, the vapor fueled logistics for obtaining can with from the natural of pipeline 818
Gas logistics merges, and it can be the vapor fueled logistics from natural gas stream 808.Can be as combustion after vapor fueled logistics
Material 982 passes through the outflow system 900 of pipeline 984.
The bottoms prepared in low-temperature fractionation post 960 mainly include the LNG with trace nitrogen.The LNG stream can
With by the inflow LNG tank 986 of pipeline 988.Pipeline 988 can include the flowing for controlling LNG stream to enter LNG tank 986
Valve 990.LNG tank 986 can be stored between any one section of LNG stream.The boiling emergent gas produced in LNG tank 986
Can be flowed at pipe joint 966 by pipeline 992.At any time at point, final LNG stream 994 can use pump 998
Being transported at LNG tank 996 is used to be conveyed to market.What is produced simultaneously in final LNG stream 944 is loaded into LNG tank 996 is another
Outer boiling escaping gas 999 can be reclaimed in cooling system 800 is cascaded.
It is appreciated that the process chart of Fig. 8 A, 8B and Fig. 9 is not intended to explanation cascade cooling system 800 or system
900 include all constituents that Fig. 8 A, 8B or Fig. 9 show.Additionally, cascade cooling system 800 or system 900 can include figure
8A, 8B or Fig. 9 distinguish not shown any number of other components, and this depends on the details of particular embodiment.Not
In same embodiment, heat exchanger 820,822,824,876,878 and 922 includes the pipe of convection rate type high.This height is right
The pipe for flowing rate type can reduce equipment size and reduce in heat exchanger 820,822,824,876,878 and 922
The storage of the refrigerant of cooling is provided.Additionally, in heat exchanger 820,822,824,876,878,922 or 926 any one all
Can be included in spiral wound type unit or brazing aluminium profiles unit.
In different embodiments, compressor 830,854,866,888,884,918,930,934,942,968,972
It is centrifugal type compressor with 976.In order to reduce the loss in refrigerant to air, each compressor 830,854,866,888,
884th, 918,930,934,942,968,972 and 976 can also include reclaiming or seal leak gas recovery system.
Figure 10 A and 10B are the process charts of another cascade cooling system 1000.The cascade cooling system 1000 can be with
It is the modified version of the cascade cooling system 800 of Fig. 8 A and 8B.Similar numeric item is carried out according to the project related to Fig. 8 A and 8B
Description.The cascade cooling system 1000 can be implemented in hydrocarbon system of processing.
Cascade cooling system 1000 can include the first fluorocarbons refrigeration system 1002, and as shown in Figure 10 A, it can be with
Use the first fluorocarbons refrigerant, such as R-410A.Cascade cooling system 1000 can also include the second fluorocarbons
Refrigeration system 1004, as shown in Figure 10 B, it can use the second fluorocarbons refrigerant, such as R-508B.Additionally, cascade
Cooling system 1000 can include nitrogen refrigeration system 1006, as shown in Figure 10 B.
The first fluorocarbons refrigeration system 1002 of Figure 10 A can be with the first fluorocarbons refrigeration system of Fig. 8 A
802 are similar to.But, the first fluorocarbons refrigeration system 1002 of Figure 10 A can be changed including the second heat exchanger 1008 and the 3rd
Hot device 1010 replaces the heat exchanger 822,824 in the first fluorocarbons refrigeration system 802 of Fig. 8 A.
In the first fluorocarbons refrigeration system 1002, by the fluorine carbon compound of the second fluorocarbons refrigeration system 1004
Thing refrigerant is by flowing through heat exchanger 820,1008 and 1010 and respectively precooling, condensation and being subcooled.The fluorocarbons refrigerant
Can be HFC, such as R-508B, or any other suitable type fluorocarbons.The fluorocarbons
Refrigerant can flow to the first fluorocarbons refrigeration system by pipeline 870 from the second fluorocarbons refrigeration system 1004
Heat exchanger 820,1008 and 1010 in 1002.Thus, the first fluorocarbons refrigeration system 1002 of Figure 10 A can provide ratio
The a greater degree of precooling of first fluorocarbons refrigeration system 802 of Fig. 8 A and smaller to the second fluorocarbons refrigerant
Compression, because the fluorocarbons refrigerant flows through all three heat exchangers 802,1008 and 1010.
Natural gas stream chilling step by step in each of heat exchanger 820,1008 and 1010.The natural gas stream of chilling it
The second fluorocarbons refrigeration system 1004 is flowed into by pipeline 874 afterwards, as shown in Figure 10 B.Second fluorocarbons refrigeration system
System 1004 can include the 4th heat exchanger 876 and the 5th heat exchanger 1012, and it can be further using fluorocarbons refrigerant
Cooled natural gas logistics.
Fluorocarbons refrigerant can continuously cycle through the second refrigeration system 1004, and it is prepared for entering heat exchange
Fluorocarbons refrigerant of the device 876 and 1012 in each.Fluorocarbons refrigerant can be as steam fluorocarbons system
Refrigerant stream leaves the 4th heat exchanger 876.The steam fluorocarbon refrigerant logistics can freeze with another steam fluorocarbons
Agent logistics merges in pipe joint 880, and can be with another steam fluorocarbon refrigerant from the 5th heat exchanger 1012
Logistics merges in pipe joint 882.Compressor 884 can be flowed through after the steam fluorocarbons refrigerant stream, it can
To increase the pressure of steam fluorocarbons refrigerant stream.Then the steam can flow through the first fluorine and be carbonized by pipeline 870
First Heat Exchanger 820 in compound refrigeration system 1002.
Once fluorocarbons refrigerant stream passes through heat exchanger 820,1008 and 1010, fluorocarbons refrigerant stream
The 3rd flash tank 1013 that can be entered in the second fluorocarbons refrigeration system 1004 by pipeline 1014.Pipeline 1014 can be with
Including expansion valve 908, its control fluorocarbons refrigerant stream enters the flowing of the 3rd flash tank 1013.Expansion valve 908 can
To reduce the temperature and pressure of fluorocarbons refrigerant stream, this causes fluorocarbons refrigerant stream to flash as steam fluorine
Both carbon compound refrigerant stream and liquid fluorocarbon compound refrigerant stream.
Steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream can be flashed into the 3rd sudden strain of a muscle
Groove 1013 is steamed, it can separate steam fluorocarbons refrigerant stream with liquid fluorocarbon compound refrigerant stream.Steam
Gas fluorocarbons refrigerant stream can be by the inflow line joint 880 of pipeline 1016.Liquid fluorocarbon compound refrigerant thing
Stream can flow to pipe joint 910 from the 3rd flash tank 1013, and liquid fluorocarbon compound refrigerant stream can be divided into two by it
Individual single liquid fluorocarbon compound refrigerant stream.One liquid fluorocarbon compound refrigerant stream can flow through the 4th heat exchange
Device 876 and by the return line joint 880 of pipeline 912 at.Another liquid fluorocarbon compound refrigerant stream can pass through
Pipeline 914 flows through the 5th heat exchanger 1012.Pipeline 914 can also include expansion valve 916, which control liquid fluorocarbon compound system
Refrigerant stream flow into the 5th heat exchanger 1012, for example by allow fluorocarbons refrigerant stream flash, reduce temperature and
Producing steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream is carried out.From the 5th heat exchanger 1012
The steam fluorocarbons refrigerant stream for obtaining can be compressed in compressor 918 and inflow line joint 882 afterwards
In to recycle.
Natural gas stream quilt by the indirect heat exchange with fluorocarbons refrigerant stream in heat exchanger 876 and 878
After cooling, the natural gas stream can flow into nitrogen refrigeration system 1006 by pipeline 920.In different embodiments,
The nitrogen gas refrigerant logistics of nitrogen refrigeration system 1006 is each in heat exchanger 820,1008,1010,876 and 1012 by flowing through
Individual and precooling.Nitrogen gas refrigerant logistics can by pipeline 921 from nitrogen refrigeration system 1006 flow to heat exchanger 820,1008,
1010th, 876 and 1012.
In nitrogen refrigeration system 1006, natural gas stream can in the 6th heat exchanger 1018 by with nitrogen gas refrigerant
The indirect heat exchange of logistics and cool down.The nitrogen gas refrigerant logistics can continuously cycle through nitrogen refrigeration system 1006, its system
For the nitrogen gas refrigerant logistics for entering the 6th heat exchanger 1018.
Nitrogen gas refrigerant logistics from the 6th heat exchanger 1018 can connect with another nitrogen gas refrigerant logistics in pipeline
Merge in first 1020.The nitrogen gas refrigerant logistics of merging can flow through the 7th heat exchanger 926 by pipeline 928.In the 7th heat exchange
In device 926, nitrogen gas refrigerant logistics can provide cooling to the high pressure nitrogen refrigerant stream of rightabout flowing.From the 7th
The nitrogen gas refrigerant logistics of heat exchanger 926 can be compressed in the first compressor 930, be cooled down in the first quencher 932, the
Compressed in two compressors 934, cooled down in the second quencher 936, compressed and in the 3rd chilling in the 3rd compressor 1022
Cooled down in device 1024.Can be with inflow line joint 1026 after the high pressure nitrogen refrigerant stream for obtaining, it can be by elevated pressure nitrogen
Gas refrigerant stream is divided into two single high pressure nitrogen refrigerant streams.
A high pressure nitrogen refrigerant stream from pipe joint 1026 can by pipeline 921 flow through heat exchanger 820,
1008th, 1010,876 and 1012.Once leaving the 5th heat exchanger 1012, nitrogen gas refrigerant logistics can be swollen in expander 1028
It is swollen, energy is produced, and inflow line joint 1020 with the nitrogen gas refrigerant logistics for leaving the 6th heat exchanger 1018 to merge.
Other high pressure nitrogen refrigerant streams can flow through the 7th heat exchanger 926 from pipe joint 1026.The elevated pressure nitrogen
Can be expanded in expander 1030 after gas refrigerant stream, produce energy, and flow through the 6th heat exchanger 1018 so as to for
Natural gas stream provides cooling.The energy produced in expander 1028 and 1030 can be used for generating electricity or drive compressor 930,
934 or 1022 part.
Once natural gas stream is cooled down in nitrogen cooling system 1006, natural gas stream can be the form of LNG.Should
LNG stream can be by the system 900 of the inflow of pipeline 948 Fig. 9.In system 900, nitrogen can be from the LNG in NRU 902
Middle removing, and as with Fig. 9 relevant discussions, LNG stream 994 may finally be obtained.
Figure 10 C are the process charts of the selective embodiment for cascading cooling system 1000, and it has simplified nitrogen
Refrigeration system 1032.As illustrated in figure 10 c, pipe joint 1020 and 1026, the 7th heat exchanger 926, expander 1030 and quencher
932 and 936 are not included in nitrogen refrigeration system 1032.Additionally, the first compressor 930 and the second compressor 934 are merged into
Single unit, i.e. compressor 1134.In these embodiments, whole nitrogen gas refrigerant logistics is flowed through by pipeline 921
Heat exchanger 820,1008,1010,876 and 1012.Thus, these embodiments simplify the design of cascade cooling system 1000.
The energy produced in expander 1028 is used for the part for generating electricity or driving compressor 1022 or 1134.
It is appreciated that the process chart of Figure 10 A, 10B and Figure 10 C is not intended to explanation cascade cooling system 1000
Including all constituents that Figure 10 A, 10B and Figure 10 C show.Additionally, cascade cooling system 1000 can include Figure 10 A, 10B
Any number of other components not shown with Figure 10 C, this depends on the details of particular embodiment.
Figure 11 A and 11B are the process charts of another cascade cooling system 1100.The cascade cooling system 1100 is distinguished
It can be the modified version of the cascade cooling system 800 and 1000 of Fig. 8 A, 8B, 10A, 10B and 10C.Similar numeric item according to
Project Fig. 8 A, 8B, 10A, 10B related to 10C is described.Cascade cooling system 1100 can be real in hydrocarbon system of processing
Apply.
Cascade cooling system 1100 can include the first fluorocarbons refrigeration system 1102, and as shown in Figure 11 A, it can be with
Use the first fluorocarbons refrigerant, such as R-410A.The cascade cooling system 1100 can also include the second fluorine carbon compound
Thing refrigeration system 1104, as shown in Figure 11 B, it can use the second fluorocarbons refrigerant, such as R-508B.
Figure 11 C are the refrigeration certainly implemented in the cascade identical hydrocarbon system of processing of cooling system 1100 with Figure 11 A and 11B
The process chart of system 1105.Similar numeric item according to Fig. 8 A, 8B, 9, the related project of 10A, 10B, 10C, 11A and 11B
It is described.Can be used for preparing LNG from natural gas stream from refrigeration system 1105.Additionally, can be wrapped from refrigeration system 1105
Include the NRU 1106 for removing nitrogen from natural gas stream.
Natural gas stream 808 can flow through quencher 810, and it makes natural gas stream by the indirect heat exchange with cooling fluid
808 precoolings.Then the natural gas stream 808 flows into the pipe joint 812 in cascade cooling system 1100.Pipe joint 812 can
To be configured to for natural gas stream 808 to be divided into three independent natural gas streams.First natural gas stream can be by pipeline 814
Inflow line joint 1107, and the second natural gas stream and the 3rd natural gas stream can be flowed into by pipeline 816 and 818 respectively
From refrigeration system 1105.
In pipe joint 1107, natural gas stream can with by pipeline 1108 from the first returned from refrigeration system 1105
Alkane recirculation stream merges.First for preparing and being cooled down for natural gas stream can be flowed into after the natural gas stream of merging
In fluorocarbons refrigeration system 1102.The natural gas stream can be by through in the first fluorocarbons refrigeration system 1102
A series of heat exchangers 1110,822 and 824 and cool down.The natural gas stream can be in each of heat exchanger 1110,822 and 824
Cooled down by the indirect heat exchange with the fluorocarbons refrigerant of circulation in individual, as related Fig. 8 A are discussed.
Then the natural gas stream for cooling down is flowed into the second fluorocarbons refrigeration system 1104 by pipeline 874, is such as schemed
Shown in 11B.Second fluorocarbons refrigeration system 1104 can include the 4th heat exchanger 1112 and the 5th heat exchanger 1114, and it can
Further to use fluorocarbons refrigerant cooled natural gas logistics.
Fluorocarbons refrigerant can be continuously circulated through the second refrigeration system 1104, and it is prepared for being changed for entrance
The fluorocarbons refrigerant of each in hot device 1112 and 1114.The fluorocarbons refrigerant can be as steam fluorine carbon
Compound refrigerant stream leaves the 4th heat exchanger 1112.Steam fluorocarbons refrigerant stream can be with another steam fluorine
Carbon compound refrigerant stream merges in pipe joint 880, and can be with another steaming from the 5th heat exchanger 1114
Gas fluorocarbons refrigerant stream merges in pipe joint 882.Flowed through after the steam fluorocarbons refrigerant stream
Compressor 884, its pressure that can increase steam fluorocarbons refrigerant stream.Then the steam can be by pipeline 870
Flow through the First Heat Exchanger 1110 in the first fluorocarbons refrigeration system 1102.
Once fluorocarbons refrigerant stream passes through heat exchanger 1110,822 and 824, the fluorocarbons refrigerant thing
The 3rd flash tank 1013 that stream can be entered in the second fluorocarbons refrigeration system 1104 by pipeline 1014.Pipeline 1014 can
Including expansion valve 908, the 3rd flash tank 1013 is flowed into which control fluorocarbons refrigerant stream.Expansion valve 908 can be with
The temperature and pressure of fluorocarbons refrigerant stream is reduced, causes fluorocarbons refrigerant stream to flash for steam fluorine is carbonized
Both compound refrigerant stream and liquid fluorocarbon compound refrigerant stream.
Steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream can be flashed into the 3rd sudden strain of a muscle
Steam in groove 1013, it can separate steam fluorocarbons refrigerant stream with liquid fluorocarbon compound refrigerant stream.
The steam fluorocarbons refrigerant stream can be by the inflow line joint 880 of pipeline 1016.Liquid fluorocarbon compound freezes
Agent logistics can be flowed at pipe joint 910 from the 3rd flash tank 1013, and it can be by liquid fluorocarbon compound refrigerant stream
It is divided into two independent liquid fluorocarbon compound refrigerant streams.One liquid fluorocarbon compound refrigerant stream can flow through
Four heat exchangers 1112 and by the return line joint 880 of pipeline 912 at.Another liquid fluorocarbon refrigerant stream can pass through
Pipeline 914 flows through the 5th heat exchanger 1114.Pipeline 914 can also include that control liquid fluorocarbon compound refrigerant stream flows into the
The expansion valve 916 of five heat exchangers 1114, such as by allowing fluorocarbons refrigerant stream to flash, reducing temperature and produce
Steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream are carried out.From the 5th heat exchanger 1114
To steam fluorocarbons refrigerant stream can be compressed in compressor 918 and afterwards inflow line joint 882 so as to
Recycling.
Natural gas stream in heat exchanger 1112 and 1114 by with fluorocarbons refrigerant stream indirect heat exchange and it is cold
But after, natural gas stream can be flowed into from refrigeration system 1105 by pipeline 1116.More particularly, the natural gas stream can be with
Flow into from the 6th heat exchanger 1118 of refrigeration system 1105.In the 6th heat exchanger 1118, the natural gas stream can pass through
With rightabout flow lower temperature natural gas stream indirect heat exchange and cool down.
Natural gas stream from the 6th heat exchanger 1118 can be with inflow line joint 1120, and be divided into for natural gas stream by it
Two single natural gas streams.One natural gas stream can flow through expansion valve 1122, and it can reduce the natural gas stream
Temperature and pressure.The 6th heat exchanger 1118 can be flowed into by pipeline 1124 after cryogenic natural gas logistics, and can used
Natural gas stream in the 6th heat exchanger 1118 is cooled down.Natural gas stream from the 6th heat exchanger 1118 can be with inflow line
Joint 1126, wherein it can merge with another natural gas stream.The natural gas stream of the merging can be in compressor 1128
Middle compression and flow into the pipe joint 1107 in the first fluorocarbons refrigeration system 1102 afterwards.
Other natural gas streams from pipe joint 1120 can be flowed into other pipe joints 1130, and wherein it can be with
Merge with another natural gas stream.The natural gas stream of merging can flow into NRU 1106 to be removed from the natural gas stream
Remove excessive nitrogen.Particularly, during natural gas stream can flow into reboiler 954, its temperature that can reduce natural gas stream.
The natural gas stream of cooling can be expanded in hydraulic expansion turbine 986 and flow through expansion valve 988 afterwards, and the valve is reduced
The temperature and pressure of natural gas stream.
Natural gas stream can be flowed into the low-temperature fractionation post 960 in NRU 1106.Additionally, heat can be by pipeline
962 pass to low-temperature fractionation post 960 from reboiler 954.The low-temperature fractionation post 960 can by low temperature distillation process by nitrogen with
Natural gas stream is separated.Overhead stream can flow out low-temperature fractionation post 960 by pipeline 964.Overhead stream can mainly include
Methane, nitrogen and other low boilings or uncondensable gas, the helium for example separated from natural gas stream.
In some embodiments, during overhead stream flows into evaporator overhead condenser 1132, it can be with separation top logistics
Any liquid and it is set to be used as during backflow returns to low-temperature fractionation post 960 by pipeline 1134.This can cause to prepare a kind of steam
Logistics, the main fuel stream including methane and the main another steam stream including low-boiling point gas.Fuel stream can be with
7th heat exchanger 1136 is flowed through by pipeline 964.In the 7th heat exchanger 1136, the temperature of vapor fueled logistics can by with
The indirect heat exchange of the natural gas stream from pipeline 816 and raise, prepare vapor fueled logistics.The vapor fueled logistics can be
Compression and chilling in a series of compressors 1138 and 1140 and quencher 1142 and 1144.The vapor fueled logistics for obtaining can be with
Merge with the natural gas stream from pipeline 818 in pipe joint 980, it can be the steam from natural gas stream 808
Fuel stream.Can be used as fuel 982 by pipeline 984 after the vapor fueled logistics to flow out from refrigeration system 1105.
The bottoms prepared in low-temperature fractionation post 960 mainly include the LNG with trace nitrogen.The bottoms can
Evaporator overhead condenser 1132 is flowed through with by pipeline 1146.Pipeline 1146 can also include that control bottoms flow into evaporator overhead condenser
1132 expansion valve 1148.The bottoms can serve as the refrigerant for evaporator overhead condenser 1132.
The mixed phase stream for obtaining from evaporator overhead condenser 1132 can flow into the first flash tank by pipeline 1152
1150.Mixed phase stream can be divided into the main steam stream including natural gas and LNG stream by first flash tank 1150.Should
Steam stream can be with inflow line joint 1154.Pipe joint 1154 can make the steam stream with another by the second flash distillation
The steam stream that groove 1156 is reclaimed merges.The steam stream of merging can flow into compressor 1158 by pipeline 1160.From pressure
The natural gas stream of contracting machine 1158 can be with inflow line joint 1126.
LNG stream from the first flash tank 1150 can flow into the second flash tank 1156 by pipeline 1162.Pipeline
1162 can include that control LNG stream flows into the expansion valve 1164 of the second flash tank 1156, and it allows one from LNG stream
Divide liquid flashes, produce the mixing phase system for flowing into the second flash tank 1156.
Mixed phase stream can be separated into LNG and steam stream including natural gas by the second flash tank 1156.The steam
Logistics can be by the inflow line joint 1166 of pipeline 1168.Pipe joint 1166 can make steam stream and by the 3rd flash tank
The 1170 another steam streams for reclaiming merge.The steam stream of the merging can compress in compressor 1172 and flow into pipe
In wire terminal 1154.
Then LNG stream is by the 3rd flash tank 1170 of inflow of pipeline 1174.Pipeline 1174 can include control LNG things
Stream flows into the expansion valve 1176 of the 3rd flash tank 1170, and it allows a part of liquid flashes from LNG.3rd flash tank 1170
The temperature and pressure of LNG stream can further be reduced so that LNG stream is close to equilibrium temperature and pressure.The steam thing of preparation
Stream can be with inflow line joint 1178, and it can be such that steam stream is closed with the boiling escaping gas reclaimed from LNG tank 1180
And.The steam stream of merging can be in compression in compressor 1182 and inflow line joint 1166.
LNG stream can be by the inflow LNG tank 1180 of pipeline 1184.The LNG tank 1180 can store one section of LNG stream
Time.The boiling escaping gas produced in LNG tank 1180 can be flowed at pipe joint 1178 by pipeline 1186.It is in office
How on time point, final LNG stream 994 can be transported in LNG tank 996 using pump 998, for transporting to market.Will
Final LNG stream 994 is loaded into other boiling escaping gas 999 produced simultaneously in LNG tank 946 and can be cooled down in cascade
Reclaimed in system 1100.
It is appreciated that Figure 11 A, 11B and 912 process chart be not intended to explanation cascade cooling system 1100 or
Include all constituents that Figure 11 A, 11B or 11C show from refrigeration system 1105.Additionally, cascade cooling system 1100 or from
Refrigeration system 1105 can respectively include the not shown any number of other components of Figure 11 A, 11B or 11C, and this is depended on
The details of particular embodiment.
Fig. 8 A and 8B；10A, 10B and 10C；System in the respective cascade cooling systems 800,1000 and 1100 of 11A and 11B
The pressure of refrigerant stream can have significant change.In some embodiments, minimum refrigerant pressure is slightly above local air
Pressure, but it can also be vacuum.In other embodiments, minimum refrigerant pressure is between about 7-9ps ia.This drop
Low coolant temperature, improves the load of fluorocarbons refrigeration system, but be reduction of nitrogen refrigeration system or methane from
The load of refrigeration system.In some embodiments, being used below the pressure of atmospheric pressure allows refrigerant energy in different fluorine
Moved in carbon compound refrigeration system, it is allowed to the use of load balance and more exercisable drivers.For example, in some situations
In, refrigerant driver can be identical for all of fluorocarbons refrigeration system and nitrogen refrigeration system.
The method for forming LNG
Figure 12 is the process chart for forming the method 1200 of LNG from natural gas stream.Method 1200 can be with office
What implement in the hydrocarbon system of processing of suitable type.Method 1200 starts at module 1202, and natural gas stream is first in this place
Cooled down in fluorocarbons refrigeration system.The first fluorocarbons refrigeration system can be mechanical refrigeration system, valve expansion
System, turbine expansion system or similar system.First fluorocarbons refrigeration system using the first fluorocarbons refrigerant with
Just cooled natural gas logistics.First fluorocarbons refrigerant for example can be hydrofluorocarbon refrigerants, such as R-410A,
Or the fluorocarbon refrigerant of any suitable type.
In different embodiments, the first fluorocarbons refrigerant is compressed to provide the first fluorine carbon of compression
Compound refrigerant, and compress the first fluorocarbons refrigerant cooled down by the indirect heat exchange with cooling fluid.Pressure
First fluorocarbons refrigerant of contracting can be expanded to cool down the first fluorocarbons refrigerant of the compression, thus prepared
Expansion, cooling the first fluorocarbons refrigerant.The expansion, cooling the first fluorocarbons refrigerant can be passed through
Heat exchange area, it can be the heat exchanger of any suitable type, such as quencher or evaporator.Additionally, natural gas stream can be with
It is compressed and cools down by the indirect heat exchange with outside cooling fluid.Then the natural gas stream can make in heat exchange area
With expansion, cooling the first fluorocarbons refrigerant chilling.
First fluorocarbons refrigeration system can also include that any number of extra cooling stages are used to cool down naturally
Gas logistics.For example, the first fluorocarbons refrigeration system can be three stage refrigeration systems, it includes that three heat exchange areas are used for
By with the first fluorocarbons refrigerant indirect heat exchange and cooled natural gas.
In module 1204, natural gas stream is cooled down in the second fluorocarbons refrigeration system.Second fluorocarbons
Refrigeration system can be mechanical refrigeration system, valve expansion system, turbine expansion system or similar system.Second fluorocarbons
Refrigeration system is using the second fluorocarbons refrigerant so as to cooled natural gas logistics.Second fluorocarbons refrigerant for example may be used
To be hydrofluorocarbon refrigerants, such as R-508B, or any other suitable type fluorocarbons refrigerant.
In different embodiments, the second fluorocarbons refrigerant is compressed to provide the second fluorine carbon of compression
Compound refrigerant, and the second fluorocarbons refrigerant for compressing is by the indirect heat exchange cooling with cooling fluid.Pressure
Second fluorocarbons refrigerant of contracting can be expanded to cool down the second fluorocarbons refrigerant of the compression, thus prepared
Expansion, cooling the second fluorocarbons refrigerant.The expansion, cooling the second fluorocarbons refrigerant can be passed through
Heat exchange area, it can be the heat exchanger of any suitable type, such as quencher or evaporator.Additionally, natural gas stream can be with
It is compressed and cools down by with outside cooling fluid indirect heat exchange.Then the natural gas stream can be used in heat exchange area
Expansion, cooling the second fluorocarbons refrigerant chilling.
Second fluorocarbons refrigeration system can also include that any number of extra cooling stages are used to cool down naturally
Gas logistics.For example, the second fluorocarbons refrigeration system can be two benches refrigeration system, it includes that two heat exchange areas are used for
By with the second fluorocarbons refrigerant indirect heat exchange and cooled natural gas.In addition, the second fluorocarbons refrigerant can be with
The precooling in the first fluorocarbons refrigeration system.For example this can flow through the first fluorine by making the second fluorocarbons refrigerant
Implement heat exchange area in carbon compound refrigeration system.
In module 1206, by natural gas stream liquefaction to form LNG in nitrogen refrigeration system.Nitrogen gas refrigerant can
For the liquefied natural gas in nitrogen refrigeration system.The nitrogen gas refrigerant can keep gas phase in nitrogen refrigeration system.
In different embodiments, nitrogen compresses and chilling in a series of compressor and quencher, swollen in hydraulic expansion turbine
It is swollen so as to the temperature for producing energy and reduce nitrogen gas refrigerant, and flow through heat exchanger.In heat exchanger, nitrogen gas refrigerant can
With by natural gas stream liquefaction with become by with natural gas stream indirect heat exchange and prepare LNG.
In module 1208, nitrogen is removed from LNG in NRU.NRU can include low-temperature fractionation post, such as NRU towers.
The nitrogen separated from LNG can flow out low-temperature fractionation post as overhead stream, and LNG can flow out as bottoms
Low-temperature fractionation post.Additionally, the liquid material from nitrogen deliverying unit bottom can be used for returning at the top of nitrogen deliverying unit
Flow condenser provides cooling.
It should be understood that the step of process chart of Figure 12 is not intended to illustration method 1200 is according to any specific
Order is performed, or explanation all includes all steps in every kind of situation.Additionally, any number of extra step can also
It is included in method 1200, this depends on the details of particular embodiment.
Figure 13 is the process chart for forming another method 1300 of LNG by natural gas stream.Similar numeric item
It is described according to the project related to Figure 12.Method 1300 can be implemented in the hydrocarbon system of processing of any suitable type.Side
Method 1300 is included in cooled natural gas in the first fluorocarbons refrigeration system at module 1202, and at module 1204
Cooled natural gas in second fluorocarbons refrigeration system.
Additionally, in module 1302, by natural gas stream cooling to form LNG from refrigeration system in methane.The first
Alkane can include that multiple expansion valves and flash tank are used for cooled natural gas from refrigeration system.In some embodiments, methane from
Refrigeration system be related Figure 11 C discuss from refrigeration system 1105.Additionally, in some embodiments, nitrogen deliverying unit
Positioned at methane from the upstream of refrigeration system.
It should be understood that the process chart of Figure 13 can be according to any special the step of being intended to illustration method 1300
Order is carried out, or all steps can be included in every kind of situation.Additionally, any amount of additional step can be wrapped
Include in method 1300, this depends on the details of particular embodiment.
Embodiment
Embodiment of the present invention can include any joint of method and system shown in following numbering paragraph.This is simultaneously
It is not considered as that it lists all possible embodiment completely, because the mode of texturing of any numbering can be retouched by of the invention
Expectation is stated to obtain.
1. one kind is used to be formed the hydrocarbon system of processing of liquefied natural gas (LNG), and it includes：
It is configured so that the first fluorocarbons refrigeration system of the first fluorocarbons refrigerant chilling natural gas；
It is configured so that the second fluorocarbons refrigeration system of the further chilling natural gas of the second fluorocarbons refrigerant
System；
Nitrogen gas refrigerant cooled natural gas are configured so as to prepare the nitrogen refrigeration system of LNG；And
It is configured to be removed from LNG the nitrogen deliverying unit of nitrogen.
2. the hydrocarbon system of processing of paragraph 1, wherein the first fluorocarbons refrigerant system configuration is the second fluorine carbon compound of cooling
Second fluorocarbons refrigerant of thing refrigeration system.
3. the hydrocarbon system of processing of paragraph 1 or 2, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration
System or be configured to cool down nitrogen refrigeration system nitrogen gas refrigerant.
4. in paragraph 1-3 either segment hydrocarbon system of processing, wherein the first fluorocarbons refrigeration system or the second fluorine carbonization
Compound refrigeration system or the two comprising it is multiple cooling circulation.
5. in paragraph 1-4 either segment hydrocarbon system of processing, wherein nitrogen refrigeration system is configured to allow to pass through including multiple
Indirect heat exchange between natural gas and nitrogen gas refrigerant and the heat exchanger of cooled natural gas.
6. in paragraph 1-5 either segment hydrocarbon system of processing, wherein the first fluorocarbons refrigeration system includes：
It is configured to compress compression of the first fluorocarbons refrigerant to provide the first fluorocarbons refrigerant of compression
Machine；
It is configured to pass the urgency that the first fluorocarbons refrigerant of the compression is cooled down with the indirect heat exchange of cooling fluid
Cooler；
It is configured to make the first fluorocarbons refrigerant of compression to expand to cool down the first fluorocarbons of the compression
The valve of refrigerant, thus prepares the first fluorocarbons refrigerant of cooling；And
Be configured to pass with cooling the first fluorocarbons refrigerant indirect heat exchange and cooled natural gas heat exchanger.
7. in paragraph 1-6 either segment hydrocarbon system of processing, wherein the second fluorocarbons refrigeration system includes：
It is configured to compress compression of the second fluorocarbons refrigerant to provide the second fluorocarbons refrigerant of compression
Machine；
It is configured to pass the urgency that the second fluorocarbons refrigerant of the compression is cooled down with the indirect heat exchange of cooling fluid
Cooler；
It is configured to make the second fluorocarbons refrigerant of compression to expand to cool down the second fluorocarbons of the compression
The valve of refrigerant, thus prepares the second fluorocarbons refrigerant of cooling；And
Be configured to pass with cooling the second fluorocarbons refrigerant indirect heat exchange and cooled natural gas heat exchanger.
8. in paragraph 1-7 either segment hydrocarbon system of processing, wherein the first fluorocarbons refrigerant include R-410A.
9. in paragraph 1-8 either segment hydrocarbon system of processing, wherein the second fluorocarbons refrigerant include R-508B.
10. in paragraph 1-9 either segment hydrocarbon system of processing, wherein the first fluorocarbons refrigerant or the second fluorine carbon compound
Thing refrigerant, or the two include non-toxic, non-combustible refrigerant.
The hydrocarbon system of processing of either segment in 11. paragraph 1-10, wherein the first fluorocarbons refrigeration system or the second fluorine carbon
Compound refrigeration system, or the two includes two or more quenchers and two or more compressors.
The hydrocarbon system of processing of either segment in 12. paragraph 1-11, wherein the first fluorocarbons refrigeration system and the second fluorine carbon
The series connection of compound refrigeration system is implemented.
The hydrocarbon system of processing of either segment in 13. paragraph 1-12, wherein nitrogen gas refrigerant is gas phase.
The hydrocarbon system of processing of either segment in 14. paragraph 1-13, wherein nitrogen refrigeration system include two or more chillings
Device, two or more expanders and two or more compressors.
The hydrocarbon system of processing of either segment in 15. paragraph 1-14, wherein the hydrocarbon system of processing are configured to chilling for carrying out hydrocarbon
The natural gas of dew point control.
The hydrocarbon system of processing of either segment in 16. paragraph 1-15, wherein the hydrocarbon system of processing are configured to chilling for natural gas
The natural gas of liquid extraction.
The hydrocarbon system of processing of either segment in 17. paragraph 1-16, wherein the hydrocarbon system of processing are configured to methane and lightweight gas
Body is separated with carbon dioxide and heavy gas.
The hydrocarbon system of processing of either segment in 18. paragraph 1-17, wherein the hydrocarbon system of processing are configured to prepare for the stone that liquefies
The hydrocarbon of production of hydrocarbons storage.
The hydrocarbon system of processing of either segment in 19. paragraph 1-18, wherein the hydrocarbon system of processing are configured to condensing reflux logistics.
A kind of 20. methods for forming liquefied natural gas (LNG), it includes：
The cooled natural gas in the first fluorocarbons refrigeration system；
The cooled natural gas in the second fluorocarbons refrigeration system；
Liquefied natural gas is forming LNG in nitrogen refrigeration system；And
Nitrogen is removed from LNG in nitrogen deliverying unit.
The method of 21. paragraphs 20, it cools down the second fluorocarbons system in being included in the first fluorocarbons refrigeration system
Second fluorocarbons refrigerant of cooling system.
The method of 22. paragraphs 20 or 21, it is included in the first fluorocarbons refrigeration system or the second fluorocarbons system
Cooling system, or the nitrogen gas refrigerant of nitrogen refrigeration system is cooled down in the two.
The method of either segment in 23. paragraph 20-22, wherein the cooled natural gas bag in the first fluorocarbons refrigeration system
Include：
The first fluorocarbons refrigerant is compressed to provide the first fluorocarbons refrigerant of compression；
The first fluorocarbons refrigerant of the compression is optionally cooled down by the indirect heat exchange with cooling fluid；
The first fluorocarbons refrigerant of compression is set to expand to cool down the first fluorocarbons refrigerant of compression, by
This prepares expansion, the first fluorocarbons refrigerant of cooling；
The first fluorocarbons refrigerant of the expansion, cooling is set to pass through the first heat exchange area；
Optional compressed natural gas；
The cooled natural gas optionally by the indirect heat exchange with outside cooling fluid；And
Make natural gas with expansion, the first fluorocarbons refrigerant heat exchanger of cooling.
The method of either segment in 24. paragraph 20-23, wherein the cooled natural gas bag in the second fluorocarbons refrigeration system
Include：
The second fluorocarbons refrigerant is compressed to provide the second fluorocarbons refrigerant of compression；
The second fluorocarbons refrigerant of the compression is optionally cooled down by the indirect heat exchange with cooling fluid；
The second fluorocarbons refrigerant of compression is set to expand to cool down the second fluorocarbons refrigerant of compression, by
This prepares expansion, the second fluorocarbons refrigerant of cooling；
The second fluorocarbons refrigerant of the expansion, cooling is set to pass through the first heat exchange area；
Optional compressed natural gas；
The cooled natural gas optionally by the indirect heat exchange with outside cooling fluid；And
Make natural gas with expansion, the second fluorocarbons refrigerant heat exchanger of cooling.
The method of either segment in 25. paragraph 20-24, it includes making nitrogen refrigeration system using one or more expansion turbines
Nitrogen gas refrigerant remain gas phase.
The method of either segment in 26. paragraph 20-25, it is included in the first fluorocarbons refrigeration system or the carbonization of the second fluorine
Compound refrigeration system, or two or more cooling stages chilling natural gases are used in the two.
The method of either segment in 27. paragraph 20-26, it uses one or more ranks of freezing in being included in nitrogen refrigeration system
Section liquefied natural gas.
The method of either segment in 28. paragraph 20-27, it includes using heat exchanger to cool down the first fluorocarbons refrigeration system
The first fluorocarbons refrigerant or the second fluorocarbons refrigeration system the second fluorocarbons refrigerant, or cooling
The two.
The method of either segment in 29. paragraph 20-28, it includes that the nitrogen for using heat exchanger to cool down nitrogen refrigeration system freezes
Agent.
A kind of 30. hydrocarbon systems of processing for forming liquefied natural gas (LNG), it includes：
The first refrigeration system of the first fluorocarbons refrigerant cooled natural gas is configured so that, wherein first refrigeration
System includes that multiple is configured to allow cool down day by the indirect heat exchange between natural gas and the first fluorocarbons refrigerant
The First Heat Exchanger of right gas,
The second refrigeration system of the second fluorocarbons refrigerant chilling natural gas is configured so that, wherein second refrigeration
System includes that multiple is configured to allow cool down day by the indirect heat exchange between natural gas and the second fluorocarbons refrigerant
Second heat exchanger of right gas；
It is configured so that threeth refrigeration system of the nitrogen gas refrigerant by natural gas adsorption LNG, wherein the 3rd refrigeration system
It is configured to allow the 3rd heat exchange of the cooled natural gas by the indirect heat exchange between natural gas and nitrogen gas refrigerant including multiple
Device；And
It is configured to be removed from LNG the nitrogen deliverying unit of nitrogen.
The hydrocarbon system of processing of 31. paragraphs 30, wherein nitrogen gas refrigerant are gas phases.
The hydrocarbon system of processing of 32. paragraphs 30 or 31, plurality of First Heat Exchanger include be configured to pass from natural gas to
The heat transfer of the first fluorocarbons refrigerant and at least partly evaporate the first fluorocarbons refrigerant with cooled natural gas
Evaporator.
The hydrocarbon system of processing of 33. paragraph 30-32, plurality of second heat exchanger includes being configured to pass from natural gas to the
The heat transfer of two fluorocarbons refrigerants and at least partly evaporate the second fluorocarbons refrigerant with the steaming of chilling natural gas
Hair device.
A kind of 34. hydrocarbon systems of processing for forming liquefied natural gas (LNG), it includes：
It is configured so that the first fluorocarbons refrigeration system of the first fluorocarbons refrigerant chilling natural gas；
It is configured so that the second fluorocarbons refrigeration system of the further chilling natural gas of the second fluorocarbons refrigerant
System；And
Cooled natural gas are configured to prepare the methane of LNG from refrigeration system.
The hydrocarbon system of processing of 35. paragraphs 34, it includes nitrogen deliverying unit of the methane from refrigeration system upstream.
The hydrocarbon system of processing of 36. paragraphs 34 or 35, wherein methane include multiple expansion valves and multiple flash distillations from refrigeration system
Groove.
Although technology of the invention can allow to improve and alternative forms, the embodiment discussed in the present invention is only led to
The mode for crossing embodiment shows.However, it should again be understood that be that these technologies are not intended to limit be spy disclosed by the invention
Different embodiment.In fact, technology of the invention includes falling with the true spirit and model of appended claims of the present invention
Alternative, improved form and the equivalent form of value in enclosing.
Claims (19)
1. a kind of hydrocarbon system of processing for forming liquefied natural gas LNG, it includes：
It is configured so that the first fluorocarbons refrigeration system of the first fluorocarbons refrigerant chilling natural gas；
It is configured so that the second fluorocarbons refrigeration system of the further chilling natural gas of the second fluorocarbons refrigerant；
Nitrogen gas refrigerant cooled natural gas are configured so as to prepare the nitrogen refrigeration system of LNG, wherein nitrogen gas refrigerant is in nitrogen
Gas phase is remained in gas refrigeration system, and wherein nitrogen refrigeration system includes two or more quenchers, two or more
Produce the expander and two or more compressors of energy；And
It is configured to be removed from LNG the nitrogen deliverying unit of nitrogen.
2. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigerant system configuration is the second fluorine carbon compound of cooling
Second fluorocarbons refrigerant of thing refrigeration system.
3. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system
Unite or be configured to the nitrogen gas refrigerant of cooling nitrogen refrigeration system.
4. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system
Unite or the two includes multiple cooling circulation.
5. the hydrocarbon system of processing of claim 1, wherein nitrogen refrigeration system is configured to allow by natural gas and nitrogen including multiple
Indirect heat exchange between gas refrigerant and the heat exchanger of cooled natural gas.
6. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigeration system includes：
It is configured to compress compressor of the first fluorocarbons refrigerant to provide the first fluorocarbons refrigerant of compression；
It is configured to pass the quencher that the first fluorocarbons refrigerant of the compression is cooled down with the indirect heat exchange of cooling fluid；
It is configured to make the first fluorocarbons refrigerant of compression to expand to cool down the first fluorocarbons refrigeration of the compression
The valve of agent, thus prepares the first fluorocarbons refrigerant of cooling；And
Be configured to pass with cooling the first fluorocarbons refrigerant indirect heat exchange and cooled natural gas heat exchanger.
7. the hydrocarbon system of processing of claim 1, wherein the second fluorocarbons refrigeration system includes：
It is configured to compress compressor of the second fluorocarbons refrigerant to provide the second fluorocarbons refrigerant of compression；
It is configured to pass the quencher that the second fluorocarbons refrigerant of the compression is cooled down with the indirect heat exchange of cooling fluid；
It is configured to make the second fluorocarbons refrigerant of compression to expand to cool down the second fluorocarbons refrigeration of the compression
The valve of agent, thus prepares the second fluorocarbons refrigerant of cooling；And
Be configured to pass with cooling the second fluorocarbons refrigerant indirect heat exchange and cooled natural gas heat exchanger.
8. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigerant includes R-410A.
9. the hydrocarbon system of processing of claim 1, wherein the second fluorocarbons refrigerant includes R-508B.
10. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigerant or the second fluorocarbons refrigerant,
Or the two includes non-toxic, non-combustible refrigerant.
The hydrocarbon system of processing of 11. claims 1, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system
Unite, or the two includes two or more quenchers and two or more compressors.
The hydrocarbon system of processing of 12. claims 1, wherein the first fluorocarbons refrigeration system and the second fluorocarbons refrigeration system
System series connection is implemented.
A kind of 13. methods for forming liquefied natural gas LNG, it includes：
The cooled natural gas in the first fluorocarbons refrigeration system；
The cooled natural gas in the second fluorocarbons refrigeration system；
Liquefied natural gas is forming LNG in nitrogen refrigeration system；
The nitrogen gas refrigerant for making nitrogen refrigeration system using one or more expansion turbines remains gas phase；And
Nitrogen is removed from LNG in nitrogen deliverying unit.
The method of 14. claims 13, it cools down the second fluorocarbons system in being included in the first fluorocarbons refrigeration system
Second fluorocarbons refrigerant of cooling system.
The method of 15. claims 13, it is included in the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system
System, or the nitrogen gas refrigerant of nitrogen refrigeration system is cooled down in the two.
The method of 16. claims 13, wherein cooled natural gas include in the first fluorocarbons refrigeration system：
The first fluorocarbons refrigerant is compressed to provide the first fluorocarbons refrigerant of compression；
The first fluorocarbons refrigerant of the compression is optionally cooled down by the indirect heat exchange with cooling fluid；
The first fluorocarbons refrigerant of compression is expanded to cool down the first fluorocarbons refrigerant of compression, thus make
Standby expansion, the first fluorocarbons refrigerant of cooling；
The first fluorocarbons refrigerant of the expansion, cooling is set to pass through the first heat exchange area；
Optional compressed natural gas；
The cooled natural gas optionally by the indirect heat exchange with outside cooling fluid；And
Make natural gas with expansion, the first fluorocarbons refrigerant heat exchanger of cooling.
The method of 17. claims 13, wherein cooled natural gas include in the second fluorocarbons refrigeration system：
The second fluorocarbons refrigerant is compressed to provide the second fluorocarbons refrigerant of compression；
The second fluorocarbons refrigerant of the compression is optionally cooled down by the indirect heat exchange with cooling fluid；
The second fluorocarbons refrigerant of compression is expanded to cool down the second fluorocarbons refrigerant of compression, thus make
Standby expansion, the second fluorocarbons refrigerant of cooling；
The second fluorocarbons refrigerant of the expansion, cooling is set to pass through the first heat exchange area；
Optional compressed natural gas；
The cooled natural gas optionally by the indirect heat exchange with outside cooling fluid；And
Make natural gas with expansion, the second fluorocarbons refrigerant heat exchanger of cooling.
The method of 18. claims 13, it is included in the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system
System, or two or more cooling stages chilling natural gases are used in the two.
The method of 19. claims 13, it uses one or more cooling stages to liquefy naturally in being included in nitrogen refrigeration system
Gas.
Applications Claiming Priority (3)
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| US201261727577P | 2012-11-16 | 2012-11-16 | |
| US61/727,577 | 2012-11-16 | ||
| PCT/US2013/067919 WO2014078092A1 (en) | 2012-11-16 | 2013-11-01 | Liquefaction of natural gas |
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| CN104813127A CN104813127A (en) | 2015-07-29 |
| CN104813127B true CN104813127B (en) | 2017-05-31 |
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| CN201380059674.2A Expired - Fee Related CN104813127B (en) | 2012-11-16 | 2013-11-01 | The liquefaction of natural gas |
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| US (2) | US20150285553A1 (en) |
| EP (1) | EP2920532A4 (en) |
| JP (1) | JP6338589B2 (en) |
| CN (1) | CN104813127B (en) |
| AU (1) | AU2013345176B2 (en) |
| BR (1) | BR112015009964A2 (en) |
| CA (1) | CA2890089C (en) |
| CL (1) | CL2015001052A1 (en) |
| IN (1) | IN2015DN03309A (en) |
| MX (1) | MX2015005359A (en) |
| SG (1) | SG11201503053SA (en) |
| WO (1) | WO2014078092A1 (en) |
| ZA (1) | ZA201503424B (en) |
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- 2013-11-01 CN CN201380059674.2A patent/CN104813127B/en not_active Expired - Fee Related
- 2013-11-01 WO PCT/US2013/067919 patent/WO2014078092A1/en active Application Filing
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| WO2014078092A1 (en) | 2014-05-22 |
| ZA201503424B (en) | 2017-09-27 |
| US20180172344A1 (en) | 2018-06-21 |
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| CA2890089A1 (en) | 2014-05-22 |
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| CN104813127A (en) | 2015-07-29 |
| BR112015009964A2 (en) | 2017-07-11 |
| SG11201503053SA (en) | 2015-06-29 |
| IN2015DN03309A (en) | 2015-10-09 |
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