CN104813127A - Liquefaction of natural gas - Google Patents
Liquefaction of natural gas Download PDFInfo
- Publication number
- CN104813127A CN104813127A CN201380059674.2A CN201380059674A CN104813127A CN 104813127 A CN104813127 A CN 104813127A CN 201380059674 A CN201380059674 A CN 201380059674A CN 104813127 A CN104813127 A CN 104813127A
- Authority
- CN
- China
- Prior art keywords
- fluorocarbons
- cold
- natural gas
- producing medium
- refrigeration system
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 662
- 239000003345 natural gas Substances 0.000 title claims abstract description 292
- 238000005057 refrigeration Methods 0.000 claims abstract description 341
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 306
- 239000003507 refrigerant Substances 0.000 claims abstract description 270
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 149
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 128
- 238000000034 method Methods 0.000 claims abstract description 104
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims description 137
- 229930195733 hydrocarbon Natural products 0.000 claims description 131
- 150000002430 hydrocarbons Chemical class 0.000 claims description 131
- 239000004215 Carbon black (E152) Substances 0.000 claims description 128
- 239000007788 liquid Substances 0.000 claims description 110
- 238000012545 processing Methods 0.000 claims description 93
- 239000007789 gas Substances 0.000 claims description 63
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 55
- 238000007906 compression Methods 0.000 claims description 45
- 230000006835 compression Effects 0.000 claims description 44
- 238000002360 preparation method Methods 0.000 claims description 26
- 238000011144 upstream manufacturing Methods 0.000 claims description 15
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 12
- 239000012809 cooling fluid Substances 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 10
- 239000003915 liquefied petroleum gas Substances 0.000 claims description 9
- 238000001179 sorption measurement Methods 0.000 claims description 7
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 4
- 239000000284 extract Substances 0.000 claims description 3
- 231100000252 nontoxic Toxicity 0.000 claims description 2
- 230000003000 nontoxic effect Effects 0.000 claims description 2
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 abstract description 6
- -1 fluorocarbon compound Chemical class 0.000 description 57
- 230000008569 process Effects 0.000 description 48
- 239000000203 mixture Substances 0.000 description 42
- 239000000463 material Substances 0.000 description 26
- 238000003860 storage Methods 0.000 description 18
- 238000007701 flash-distillation Methods 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 15
- 238000005194 fractionation Methods 0.000 description 15
- 229910052799 carbon Inorganic materials 0.000 description 13
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 12
- 239000000470 constituent Substances 0.000 description 11
- 239000002826 coolant Substances 0.000 description 11
- 238000009835 boiling Methods 0.000 description 10
- 238000009833 condensation Methods 0.000 description 10
- 230000005494 condensation Effects 0.000 description 10
- 229920006395 saturated elastomer Polymers 0.000 description 10
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 7
- 239000000446 fuel Substances 0.000 description 7
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 7
- 239000011555 saturated liquid Substances 0.000 description 7
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 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
- 238000013461 design Methods 0.000 description 5
- 238000000605 extraction Methods 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 5
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 4
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 4
- PRPAGESBURMWTI-UHFFFAOYSA-N [C].[F] Chemical class [C].[F] PRPAGESBURMWTI-UHFFFAOYSA-N 0.000 description 4
- 239000001273 butane Substances 0.000 description 4
- 150000001875 compounds Chemical class 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
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 4
- 238000009834 vaporization Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 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
- 150000001721 carbon Chemical group 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000000498 cooling water Substances 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
- RWRIWBAIICGTTQ-UHFFFAOYSA-N difluoromethane Chemical compound FCF RWRIWBAIICGTTQ-UHFFFAOYSA-N 0.000 description 3
- 238000004821 distillation 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
- 238000002156 mixing Methods 0.000 description 3
- 150000002829 nitrogen Chemical class 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910001868 water Inorganic materials 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
- 230000008901 benefit Effects 0.000 description 2
- 230000007423 decrease Effects 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
- 229910052731 fluorine Inorganic materials 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- 150000008282 halocarbons Chemical class 0.000 description 2
- WMIYKQLTONQJES-UHFFFAOYSA-N hexafluoroethane Chemical compound FC(F)(F)C(F)(F)F WMIYKQLTONQJES-UHFFFAOYSA-N 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000005292 vacuum distillation Methods 0.000 description 2
- INEMUVRCEAELBK-UHFFFAOYSA-N 1,1,1,2-tetrafluoropropane Chemical compound CC(F)C(F)(F)F INEMUVRCEAELBK-UHFFFAOYSA-N 0.000 description 1
- NSGXIBWMJZWTPY-UHFFFAOYSA-N 1,1,1,3,3,3-hexafluoropropane Chemical compound FC(F)(F)CC(F)(F)F NSGXIBWMJZWTPY-UHFFFAOYSA-N 0.000 description 1
- 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
- 230000004308 accommodation Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 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
- 238000005219 brazing Methods 0.000 description 1
- 230000008859 change Effects 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
- 239000000110 cooling liquid Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 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
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000002737 fuel gas Substances 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
- 230000010354 integration Effects 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
- 238000005457 optimization Methods 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
- 239000011435 rock Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 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
- 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
- 238000012546 transfer Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- 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
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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
- F25J1/005—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
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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
- F25J1/0207—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
Abstract
Systems and a method for the formation of a liquefied natural gas (LNG) are disclosed herein. The system includes a first fluorocarbon refrigeration system configured to chill a natural gas using a first fluorocarbon refrigerant and a second fluorocarbon refrigeration system configured to further chill the natural gas using a second fluorocarbon refrigerant. The system also includes a nitrogen refrigeration system configured to cool the natural gas using a nitrogen refrigerant to produce LNG and a nitrogen rejection unit configured to remove nitrogen from the LNG. As an alternative embodiment, the nitrogen refrigeration system can be replaced by a methane autorefrigeration system.
Description
The cross reference of related application
This application claims and benefit from the U.S. temporary patent application 61/727,577 that the exercise question submitted on November 16th, 2012 is " liquefaction of natural gas ", its full content is incorporated to the present invention by reference to document.
Invention field
Technology of the present invention relates generally to the field of hydrocarbon recovery and processing method, and relating more specifically to the method and system being formed liquefied natural gas (LNG) by the method for refrigeration, it is included in nitrogen kind of refrigeration cycle or two the fluorocarbons kind of refrigeration cycle of methane from kind of refrigeration cycle upstream.
Background technology
This part is intended to the many aspects introducing prior art, and it can be relevant to the exemplary of the technology of the present invention.Believe that this content of the discussions contributes to providing convenience the framework of the special aspects better understanding the technology of the present invention.Therefore, should be understood that, this part content should be read based on this point, and there is no need the statement that it can be used as prior art.
Many cryogenic refrigerating systems for natural gas processing and liquefaction all depend on the use of the cold-producing medium comprising hydrocarbon component and nitrogen to provide external refrigeration.These hydrocarbon components can comprise methane, ethane, ethene, propane and similar material.But, in many cases, can expect to use non-combustible cold-producing medium to implement refrigeration system.
The U.S. patent No.6 of the people such as Foglietta, 412,302 describe a kind of method preparing liquefied natural gas stream.The method comprises by carrying out heat exchange with the first and second refrigerant contact expanded circulated for independent cooling and cools the natural gas feed stream of pressurizeing at least partially.First swell refrigeration agent is selected from methane, ethane and process and the natural gas of pressurization, and the second swell refrigeration agent is nitrogen.But, as what discuss in the present invention, expect the LNG logistics preparing the refrigeration system inside using non-combustible cold-producing medium.
Summary of the invention
One embodiment of the invention provide a kind of hydrocarbon system of processing for the formation of liquefied natural gas (LNG).This hydrocarbon system of processing comprises the first fluorocarbons refrigeration system being configured to use first fluorocarbons cold-producing medium chilling natural gas and the second fluorocarbons refrigeration system being configured to the further chilling natural gas of use second fluorocarbons cold-producing medium.This hydrocarbon system of processing also comprises and is configured to use nitrogen gas refrigerant cooled natural gas prepare the nitrogen refrigeration system of LNG and to be configured to remove the nitrogen deliverying unit of nitrogen from LNG.
Another embodiment of the invention provides a kind of method forming LNG.The method is included in cooled natural gas in the first fluorocarbons refrigeration system, in the second fluorocarbons refrigeration system cooled natural gas, in nitrogen refrigeration system liquefied natural gas to form LNG and remove nitrogen from LNG in nitrogen deliverying unit.
Another embodiment of the invention provides a kind of hydrocarbon system of processing for the formation of LNG.This hydrocarbon system of processing comprises the first refrigeration system being configured to use first fluorocarbons refrigerant cools natural gas, wherein this first refrigeration system comprise many be configured to allow by the indirect heat exchange between natural gas and the first fluorocarbons cold-producing medium the First Heat Exchanger of cooled natural gas.This hydrocarbon system of processing comprises the second refrigeration system being configured to use second fluorocarbons cold-producing medium chilling natural gas, wherein this second refrigeration system comprise many be configured to allow by the indirect heat exchange between natural gas and the second fluorocarbons cold-producing medium the second heat exchanger of cooled natural gas.This hydrocarbon system of processing also comprises and is configured to use nitrogen gas refrigerant by the 3rd refrigeration system of natural gas adsorption LNG, and wherein the 3rd refrigeration system comprises many being configured to and allows by the indirect heat exchange between natural gas and nitrogen gas refrigerant the 3rd heat exchanger of cooled natural gas.This hydrocarbon system of processing also comprises the nitrogen deliverying unit being configured to remove nitrogen from LNG further.
Another embodiment of the invention provides a kind of hydrocarbon system of processing forming LNG.This hydrocarbon system of processing comprises the first fluorocarbons refrigeration system being configured to use first fluorocarbons cold-producing medium chilling natural gas, be configured to the second fluorocarbons refrigeration system of the further chilling natural gas of use second fluorocarbons cold-producing medium, and be configured to cooled natural gas to prepare the methane of LNG from refrigeration system.
Summary of the invention
The embodiment that the present invention describes provides a kind of hydrocarbon system of processing.This hydrocarbon system of processing comprises refrigeration system, such as cascade cooling system, to prepare LNG by natural gas.This refrigeration system comprises two fluorocarbons refrigeration systems and nitrogen or methane refrigeration systems associated.This fluorine carbon can also be used for cooled natural gas with without refrigeration system and nitrogen or methane refrigeration systems associated, thus preparation LNG.In addition, this hydrocarbon system of processing can comprise NRU, and it may be used for removing nitrogen from the LNG of preparation.
Hydrocarbon system of processing comprises the system well known by persons skilled in the art of arbitrary number.Hydrocarbon preparation and processing procedure include but not limited to that chilling natural gas extracts for NGL, and chilling natural gas is used for hydrocarbon dew point and controls, and chilling natural gas is for removing CO
2, LPG produces storage, the condensation refluxed in dethanizer/domethanizing column, and natural gas liquefaction is to prepare LNG.
Although many kind of refrigeration cycle may be used to processing hydrocarbons, a kind of circulation for LNG liquefaction plant is cascade cycle, and it uses the cold-producing medium of multiple independent component to reduce the temperature of the gases to condensing temperature in the heat exchanger arranged step by step.Another circulation for LNG liquefaction engineering is multiple group sub-refrigerating circulation, and it uses multi-component refrigrant in the interchanger of particular design.In addition, the another kind of circulation being used for LNG liquefaction engineering is expander cycle, and it makes the gas pressure from unstripped gas expand into lower pressure and has the corresponding reduction of temperature.Distortion or associating that NG Liquefaction cycle can also use these three kinds to circulate.
The LNG prepared by refrigeration and liquefaction technology by unstrpped gas.Optional step comprises removing condensate, removing CO
2, dehydration, removing mercury, removes nitrogen, removing H
2s and similar step.Post liquefaction, LNG can store or be loaded on oil tanker for selling or transport.Conventional liquifying method comprises: the hybrid refrigeration that APCI propane pre-cooling goes; C3MR; DUAL MR; The cascade of Phillips optimization; The mix refrigerant that Prico is single; The two pressure mix refrigerant of TEAL; The cascade of Linde/Statoil multi-fluid; Axens double-mixed refrigerant; DMR; With Shell technique C3MR and DMR.
Removing carbon dioxide, by methane and light gas and CO
2be separated with heavy gas, this can use cryogenic distillation method to implement, the controllable solidification district technology such as obtained by ExxonMobil Corporation.
Although the method and system that the present invention describes is about the discussion by natural gas adsorption LNG, described method and system can also be used for other object multiple.Such as method and system of the present invention may be used for chilling natural gas and controls for hydrocarbon dew point, carry out natural gas liquids (NGL) extraction, methane and light gas and carbon dioxide and heavy gas are separated, for the preparation of the hydrocarbon that LPG produces, or condensing reflux logistics etc. in dethanizer and/or domethanizing column.
Cold-producing medium
Can be one or more one-component refrigerants for the cold-producing medium according to embodiment of the present invention, or comprise multi-component refrigerant mixture.Cold-producing medium can import or stored on-site, or alternatively, some components of cold-producing medium can be prepared at the scene, and it is prepared typically by the still-process integrated with hydrocarbon system of processing.The cold-producing medium of commercially available acquisition comprises fluorocarbons (FC) or HFC (HFC), and it can be used in multiple application.Exemplary cold-producing medium can be commercially available by DuPont Corporat ion, comprises
series cold-producing medium,
series cold-producing medium,
series cold-producing medium, and
series cold-producing medium.
The commercially available acquisition of multi-component refrigrant.Such as, R-401A is the HCFC blend of R-32, R-152a and R-124.R-404A is the HFC blend of the R-134a of R-125 and 4wt.% of R-143a, 44wt.% of 52wt.%.R-406A is the blend of the R-142b of R-600a and 41wt.% of R-22,4wt.% of 55wt.%.R-407A is the HFC blend of the R-134a of R-125 and 40wt.% of R-32,40wt.% of 20wt.%.R-407C is the HFC blend of R-32, R-125 and R-134a.R-408A is the HCFC blend of R-22, R-125 and R-143a.R-409A is the HCFC blend of R-22, R-124 and R-142b.R-410A is the blend of R-32 and R-125.R-500 is the blend of the R-152a of R-12 and 26.2wt.% of 73.8wt.%.R-502 is the blend of R-22 and R-115.R-508B is the blend of R-23 and R-116.
In different embodiments, use together with any refrigeration system that the dissimilar hydrocarbon system of processing of any number can describe with the present invention.In addition, the refrigeration system that the present invention describes can be any cold-producing medium using the present invention to describe.
Refrigeration system
Hydrocarbon system and method generally include and use mechanical refrigeration, valve expands, the refrigeration system of turbine expansion or similar techniques.Mechanical refrigeration typically comprises compressibility and absorption system, such as aqua-ammonia absorption system.Compressibility is in order to various work technique is for gas processing industry.Such as, compressibility can be used for chilling natural gas for NGL extraction, chilling natural gas controls for hydrocarbon dew point, LPG produces storage, and the condensation refluxed in dethanizer or domethanizing column, natural gas liquefaction is to prepare LNG or similar operations.
Fig. 1 is the process chart of single phase refrigeration system 100.In different embodiments, single phase refrigeration system 100 use the cold-producing medium of such as fluorocarbons.In addition, in different embodiments, nitrogen refrigeration or methane that single phase, refrigeration system 100 comprised NRU are implemented from the upstream of refrigeration system.Multiple single phase, refrigeration system 100 can also implement from refrigeration system upstream tandem in this nitrogen refrigeration system or methane.
Single phase, refrigeration system 100 comprised expansion valve 102, quencher 104, compressor 106, condenser 108 and material storage container 110.Saturated liquid cold-producing medium 112 can flow to expansion valve 102 from material storage container 110, and isenthalpic expansion is through expansion valve 102.There are some evaporations during expansion, produce the refrigerant mixture 114 comprising the chilling of steam and liquid.Refrigerant mixture 114 can enter quencher 104 at the temperature that will be cooled to lower than process-stream 116, such as natural gas, and this quencher is also known to evaporimeter.Process-stream 116 flow through quencher 104 and with coolant mixture 114 heat exchange.Along with process-stream 116 and coolant mixture 114 carry out heat exchange, process-stream 116 cools, and refrigerant mixture 114 evaporates, and produces saturated vaporous cryogen 118.
After leaving quencher 104, saturated vaporous cryogen 118 is compressed in compressor 106, and flows to condenser 108 afterwards.In condenser 108, saturated vaporous cryogen 118 changes into saturated or slightly excessively cold liquid refrigerant 120.Material storage container 110 can be flowed to from condenser 108 after liquid refrigerant 120.This material storage container 110 is also known to surge tank or receiver, can be used as the holder of liquid refrigerant 120.Liquid refrigerant 120 can be stored in material storage container 110 as saturated liquid cold-producing medium 112 before expanding through expansion valve 102.
Should be understood that the process chart of Fig. 1 be not intended to instruction book stage refrigeration system 100 comprise Fig. 1 display all constituents.In addition, single phase refrigeration system 100 can comprise other parts of the arbitrary number that Fig. 1 does not show, this depends on the details of particular embodiment.Such as, in some embodiments, refrigeration system can comprise two or more compression stages.In addition, refrigeration system 100 can comprise saveall, as relevant Fig. 2 discusses further.
Fig. 2 is the process chart of the two benches refrigeration system 200 comprising saveall 202.Similar numeric item is described according to the project relevant to Fig. 1.In different embodiments, two benches refrigeration system 200 uses the cold-producing medium of such as fluorocarbons.In addition, in different embodiments, nitrogen refrigeration or methane that two benches refrigeration system 200 is comprising NRU are implemented from the upstream of refrigeration system.Multiple two benches refrigeration system 200 can also be implemented from the upstream tandem of refrigeration system in this nitrogen refrigeration system or methane.
Saveall 202 can be reduce to improve for any device of the compressor horsepower of given quencher load or method.Conventional saveall 202 such as comprises flash tank and heat exchanger saveall.Add heat exchanger and use multiple heat exchanger transmitting heat between process-stream.This can by thermally integrating process-stream and reducing the amount of the energy be input in two benches refrigeration system 200.
As shown in Figure 2, the saturated liquid cold-producing medium 112 leaving material storage container 110 can expand through expansion valve 102 and reach middle pressure, and steam can be separated with liquid at this pressure.Such as, along with saturated liquid cold-producing medium 112 flash distillation is through expansion valve 102, under the pressure and temperature lower than saturated liquid cold-producing medium 112, vaporous cryogen 204 and liquid refrigerant 206 has been prepared.Then vaporous cryogen 204 and liquid refrigerant 206 can flow in saveall 202.In different embodiments, saveall 202 carries out the flash tank that vaporous cryogen 204 is separated with liquid refrigerant 206.Vaporous cryogen 204 can flow to middle pressure compressor stage, and vaporous cryogen 204 can merge with the saturated vapor cold-producing medium 118 left from the first compressor 210 there, generates the saturated vapor cold-producing medium 208 of mixing.The second compressor 212 can be flowed to after the saturated vapor cold-producing medium 208 of mixing.
Liquid refrigerant 206 from saveall 202 can pass the second expansion valve 214 by isenthalpic expansion.Some evaporations can be there are during expansion, produce the refrigerant mixture 216 comprising steam and liquid, thus reduce temperature and pressure.Refrigerant mixture 216 will have than not having the content liquid that the refrigerant mixture in the system of saveall is higher.Higher content liquid can reduce refrigerant circulation speed and/or reduce the energy ezpenditure of the first compressor 210.
Refrigerant mixture 216 enters also known in the quencher 104 of evaporimeter at the temperature of the temperature that will be cooled to lower than process-stream 116.As discussing in relevant Fig. 1, this process-stream 116 cools in quencher 104.In addition, saturated vaporous cryogen 118 flows through compressor 210 and 212 and condenser 108, and the liquid refrigerant 120 produced is stored in material storage container 110, as discussing in relevant Fig. 1.
Be understandable that the process chart of Fig. 2 is not intended to illustrate that two benches refrigeration system 200 comprises all constituents shown in Fig. 2.In addition, two benches refrigeration system 200 can comprise other parts of the arbitrary number that Fig. 2 does not show, and this depends on the details of particular embodiment.Such as, two benches refrigeration system 200 can comprise other savealls of the arbitrary number do not shown in Fig. 2 or the equipment of other types.In addition, saveall 202 can be heat exchanger saveall instead of flash tank.Heat exchanger saveall can also reduce compressor energy ezpenditure for reducing kind of refrigeration cycle speed.
In some embodiments, two benches refrigeration system 200 comprises more than one saveall 202, and more than the compressor 210 and 212 of two.Such as, two benches refrigeration system 200 can comprise two savealls and three compressors.Usually, if refrigeration system 200 comprises X saveall, so this refrigeration system 200 will comprise X+1 compressor.This refrigeration system 200 with multiple saveall can form a part for cascade refrigeration system.
Fig. 3 be comprise heat exchanger saveall 302 single phase refrigeration system 300 process chart.Similar numeric item is described according to the project relevant to Fig. 1.In different embodiments, single phase refrigeration system 300 use the cold-producing medium of such as fluorocarbons.In addition, in different embodiments, nitrogen refrigeration or methane that single phase, refrigeration system 300 comprised NRU are implemented from the upstream of refrigeration system.Multiple single phase, refrigeration system 300 can also implement from the upstream tandem of refrigeration system in this nitrogen refrigeration system or methane.
As shown in Figure 3, the saturated liquid cold-producing medium 112 leaving material storage container 110 can expand through expansion valve 102 and reach middle pressure, and steam can be separated with liquid and prepare refrigerant mixture 114 at this pressure.This refrigerant mixture 114 can flow to quencher 104 at the temperature lower than the temperature of process for cooling logistics 116.This process-stream 116 can cool in quencher 104, as relevant Fig. 1 discusses.
Saturated vapor cold-producing medium 118 from quencher 104 can flow through heat exchanger saveall 302.Cold, low pressure saturated vapor cold-producing medium 118 may be used for making the saturated liquid cold-producing medium 112 in heat exchanger saveall 302 excessively cold.Can flow through compressor 106 and condenser 108 after heat exchanger saveall 302 superheated vapor cold-producing medium 304 out, and the liquid refrigerant 120 obtained can be stored in material storage container 110, as relevant Fig. 1 discusses.
Be understandable that the process chart of Fig. 3 is not intended to instruction book stage refrigeration system 300 and comprises all constituents shown in Fig. 3.In addition, single phase refrigeration system 300 can comprise other parts of the arbitrary number that Fig. 3 does not show, this depends on the details of particular embodiment.
Fig. 4 is the process chart of the cascade cooling system 400 comprising the first refrigeration system 402 and the second refrigeration system 404.In different embodiments, the first refrigeration system 402 and the second refrigeration system 404 employ fluorocarbons cold-producing medium.Such as, the first refrigeration system 402 can use R-410A, and the second refrigeration system 404 can use R-508B.In addition, the cold-producing medium in refrigeration system 402 or 404 can comprise mixture.Cascade cooling system 400 such as may be used for the cooling than expecting the higher degree that refrigeration system 100,200 or 300 can provide.Cascade cooling system 400 can provide the cooling under unusual low temperature, such as, lower than-40 DEG C.In addition, in some embodiments, cascade cooling system 400 is implemented from the upstream of refrigeration system in nitrogen refrigeration system or methane.
In the first refrigeration system 402, vapor/liquid refrigerant stream 406 can flow through the first expansion valve 410 and First Heat Exchanger 412 from material storage container 408, its chilling product stream 413.The steam stream obtained is separated in the first flash tank 414.Part vapor/liquid cooling agent logistics 406 can directly flow to the first flash tank 414 place by bypass valve 416.
Liquid refrigerant logistics 418 from flash tank 414 can flow through the second expansion valve 420, and flash distillation enters the second heat exchanger 422, and it may be used for further chilling product stream 413.The vaporous cryogen logistics 426 obtained is fed to first stage compressor 428 place by gas material storage container 424.The middle pressure vaporous cryogen logistics 430 obtained merges with the vaporous cryogen logistics 432 from flash tank 414, and the logistics of merging is fed to second stage compressor 434 place.Condenser 438 is passed in HCS logistics 436 from second stage compressor 434, and it can use the cooling from the second refrigeration system 404.Especially, condenser 438 can use the low-temperature refrigerant logistics 440 from the second refrigeration system 404 to cool HCS logistics 436 to prepare liquid refrigerant logistics 406.Be stored in material storage container 408 after liquid refrigerant logistics 406 from refrigeration condenser 438.By-pass valve control 442 may be used for controlling the flowing of low-temperature refrigerant logistics 440 through condenser 438.The vaporous cryogen logistics 444 obtained from refrigeration 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 heat exchanger 452 being configured to pass chilling system 454 and liquid refrigerant logistics 448 is cooled.This chilling system 454 such as can carry out heat exchange from different process-streams, such as, carry out to be separated the natural gas stream of the final flash tank of NGL in gas.
The low-temperature refrigerant logistics 456 obtained can flow through the first expansion valve 458 and First Heat Exchanger 460, its chilling product stream 413.The vapor/liquid refrigerant stream obtained is separated in the first flash tank 462.Part low-temperature refrigerant logistics 456 can directly flow to the first flash tank 462 by bypass valve 464, and this valve can be the Level control valve entering flash tank 462 for controlling fluid.
Liquid refrigerant logistics 466 from the first flash tank 462 can flow through the second expansion valve 468, and flash distillation enters the second heat exchanger 470, and it may be used for further chilling product stream 413.The vapor/liquid refrigerant stream obtained can be separated in the second flash tank 472.Part liquid refrigerant logistics 466 can flow directly into the second flash tank 472 by bypass valve 474, and this valve may be used for the fluid temperature in control second flash tank 472, and the amount of cooling water in the second heat exchanger 470.
Liquid refrigerant logistics 476 from the second flash tank 472 can flow through the 3rd expansion valve 478, and flash distillation enters the 3rd heat exchanger 480, and it may be used for further chilling product stream 413.The vaporous cryogen logistics 484 obtained is fed in first stage compressor 486 by gas material storage container 482.The middle pressure vaporous cryogen logistics 488 obtained merges with the vaporous cryogen logistics 490 from the second flash tank 472, and the logistics of merging is fed in second stage compressor 492.The HCS refrigerant stream 494 obtained merges with the vapor refrigerant mixture 496 from the first flash tank 462, and the logistics of merging is fed in phase III compressor 497.The HCS refrigerant stream 498 obtained flows through heat exchanger 499, and wherein it can cool further by with cooling water indirect heat exchange.Material storage container 450 can be flowed to after the liquid refrigerant logistics 448 obtained.
Should be understood that the process chart of Fig. 4 is not intended to illustrate that cascade cooling system 400 comprises all constituents of Fig. 4 display.In addition, cascade cooling system 400 can comprise other parts of the arbitrary number that Fig. 4 does not show, and this depends on the details of particular embodiment.
Fig. 5 is the process chart of the expansion refrigeration system 500 for hydrocarbon dew point control.Heavy hydrocarbon in natural gas in pipeline, such as C
3-C
6the condensation of heavy hydrocarbon the impact of liquid in pipeline and gas can be caused to accept breaking of facility.Therefore, hydrocarbon dew point can use expansion refrigeration system 500 to reduce, to prevent this condensation.
As shown in Figure 5, the natural gas material flow 502 of dehydration can in inflow gas/gas heat exchanger 504.In gas/gas heat exchanger 504, the natural gas material flow 502 of dehydration can be cooled by the indirect heat exchange with cryogenic natural gas logistics 506.The natural gas stream 508 obtained can flow in the first separator 510, and it can remove the heavy hydrocarbon 512 from natural gas stream 508 of a tittle.In different embodiments, the heavy hydrocarbon 512 removed from natural gas stream 508 reduces the dew point of natural gas stream 508.The heavy hydrocarbon 512 of removing can flow out expansion refrigeration system 500 by the first outlet valve 514.Such as, heavy hydrocarbon 512 can flow to stabilizer (not shown) from swell refrigeration agent system 500.
Natural gas stream 508 can flow in expander 516 afterwards.In different embodiments, expander 516 is turbine expansion devices, and it is centrifugal or axial turbine.In expander 516, the expansion of natural gas stream 508 can provide energy for driving compressor 518, and it is connected by axostylus axostyle 520 with expander 516.
The cryogenic natural gas logistics 506 obtained from expander 516 can flow to the second separator 522, and it can remove any residual heavy hydrocarbon 512 from cryogenic natural gas logistics 506.In different embodiments, from cryogenic natural gas logistics 506, remove the dew point that heavy hydrocarbon 512 reduce further cryogenic natural gas logistics 506.Then the heavy hydrocarbon 512 removed can flow out expansion refrigeration system 500 by the 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 the temperature of cryogenic natural gas logistics 506 raise, thus prepares high-temperature natural gas logistics 526.Can flow through compressor 518 after high-temperature natural gas logistics 526, it can make the pressure of natural gas stream 526 get back to the pressure of acceptable sales gas.Finally, expansion refrigeration system 500 can be flowed out after reducing the natural gas stream 528 of dew point.
In one embodiment, the cooling system of fluorocarbons cold-producing medium and nitrogen gas refrigerant is such as used to may be used for increasing the further cooling to process.This cooling by being placed in natural gas stream 508 or in cryogenic natural gas logistics 506 by heat exchanger 530, can be implemented in the upstream of the second separator 522.Refrigerant liquid 532 flash distillation can pass expansion valve 534, by quencher 530.Can get back in refrigeration system after the refrigerant vapour 536 obtained.This chilling can allow to remove the condensable hydrocarbon of more a large amount, such as C
3and higher hydrocarbon.In addition, in some embodiments, heat exchanger 530 is placed on the upstream of expander 516, and it has separator between heat exchanger 530 and expander 516 to prevent flow direction expander 516.
Be understandable that the process chart of Fig. 5 is not intended to illustrate that expansion refrigeration system 500 comprises all constituents of Fig. 5 display.In addition, expansion refrigeration system 500 can comprise other parts of the arbitrary number that Fig. 5 does not show, and this depends on the details of particular embodiment.Such as, in some embodiments, the cascade cooling system being arranged in nitrogen refrigeration system upstream that expansion refrigeration system 500 is comprising two fluorocarbons refrigeration systems is implemented.In these embodiments, flash distillation is from the fluorocarbons cold-producing medium of one of fluorocarbons refrigeration system or the nitrogen gas refrigerant from nitrogen refrigeration system through expansion valve 534 and the refrigerant liquid 532 that flows through quencher 530.
Fig. 6 is the process chart of the expansion cooling system 600 prepared for NGL.Can carry out NGL extraction to reclaim NGL, it comprises the different heavy hydrocarbons from natural gas stream of arbitrary number.NGL extraction can be expected, because the normally more valuable object of NGL instead of the fact as gas-phase heating fuel.
Dry natural gas material flow 602 can from dewatering system inflow gas/gas heat exchanger 604.In gas/gas heat exchanger 604, dry natural gas material flow 602 can by cooling with the indirect heat exchange of cryogenic natural gas logistics 606.The natural gas stream 608 obtained can flow in separator 610, its can from natural gas stream 608 remove portion NGL 612.The NGL 612 of removing can flow to dethanizer or domethanizing column 614 from separator 610.
Can flow in expander 616 after natural gas stream 608.In different embodiments, expander 616 is turbine expansion devices.Natural gas stream 608 in expander 616 can provide energy for driving compressor 618, and it is by axostylus axostyle 620 and expander 616 coupling.In addition, the temperature of natural gas stream 608 can by reducing through Joule-Thomson valve 622 carries out adiabatic expansion.
The cryogenic natural gas logistics 606 obtained from expander 616 can flow in dethanizer or domethanizing column 614.In dethanizer or domethanizing column 614, NGL can be separated and can flow out dethanizer or domethanizing column 614 as NGL product stream 624 from natural gas stream 606.Expansion refrigeration system 600 can be pumped by pump 626 after NGL product stream 624.
Dethanizer or domethanizing column 614 can be connected with heat exchanger 628.In some embodiments, heat exchanger 628 is reboilers 628, and it can by indirect heat exchange in high temperature fluid 632 for heating the bottoms 630 of a part from dethanizer or domethanizing column 614.Then the bottoms 630 heated can re-inject in dethanizer or domethanizing column 614.
That carries out in dethanizer or domethanizing column 614 is separated the preparation that NGL product stream 624 can cause cryogenic natural gas logistics from natural gas stream 606, and this logistics can flow out dethanizer or domethanizing column 614 as overhead stream 634.Overhead stream 634 can in inflow heat exchanger 636, and this heat exchanger can reduce the temperature of overhead stream 634 by the indirect heat exchange with cold-producing medium 638, such as fluorocarbons cold-producing medium or nitrogen gas refrigerant.The reduction of temperature can cause the condensation of some steams.Then overhead stream 634 can be separated to prepare cryogenic natural gas logistics 606 and liquid bottom stream 642 in separation container 640.Bottoms 642 can be pumped back in dethanizer or domethanizing column 614 by pump 644, forms recirculation stream.
Cryogenic natural gas logistics afterwards 606 can flow through gas/gas heat exchanger 604.The temperature of cryogenic natural gas logistics 506 can be raised in gas/gas heat exchanger 604, prepares high-temperature natural gas logistics 646.Can flow through compressor 618 after high-temperature natural gas logistics 646, it can increase the pressure of natural gas stream 646.In some embodiments, high-temperature natural gas logistics 646 also flows through the second compressor 648, and the pressure of natural gas stream 646 can be increased to the pressure of acceptable sales gas by it.Then gas product logistics 650 can flow out expansion refrigeration system 600.
Be understandable that the process chart of Fig. 6 is not intended to illustrate that expansion refrigeration system 600 comprises all constituents of Fig. 6 display.In addition, expansion refrigeration system 600 can comprise other parts of the arbitrary number that Fig. 6 does not show, and this depends on the details of particular embodiment.Such as, in some embodiments, the cascade cooling system that expansion refrigeration system 600 is comprising two fluorocarbons refrigeration systems and be arranged in nitrogen refrigeration system upstream is implemented.In these embodiments, the cold-producing medium 638 used in heat exchanger 636 is from the fluorocarbons cold-producing medium of one of fluorocarbons refrigeration system or the nitrogen gas refrigerant from nitrogen refrigeration system.
Fig. 7 is the process chart of LNG preparation system 700.As shown in Figure 7, LNG 702 can use multiple different refrigeration system to be prepared by natural gas stream 704.As shown in Figure 7, a part of natural gas stream 704 can be separated before entering LNG preparation system 700 from natural gas stream 704, and can be used as fuel gas stream 706.Remaining natural gas stream 704 can flow in initial gas processing system 708.In gas processing system 708, natural gas stream 704 can purifying and cooling.Such as, natural gas stream 704 can use the first fluorocarbons cold-producing medium 710, second fluorocarbons cold-producing medium 712 and high pressure nitrogen cold-producing medium 714 to cool.The cooling of natural gas stream 704 can cause the preparation of LNG 702.
In LNG preparation system 700, heavy hydrocarbon 716 can remove from natural gas stream 704, and a part of heavy hydrocarbon 716 may be used for the gasoline 718 prepared in heavy hydrocarbon system of processing 720.In addition, any residual natural gas 722 be separated from heavy hydrocarbon 716 during the preparation of gasoline 718 can be got back in natural gas stream 704.
The LNG 702 of preparation can comprise the nitrogen 724 of a tittle.Therefore, LNG 702 can flow through NRU 726.NRU 726 isolates nitrogen 724 from LNG 702, prepares final LNG product.
Be understandable that the process chart of Fig. 7 is not intended to illustrate that LNG preparation system 700 comprises all constituents of Fig. 7 display.In addition, LNG preparation system 700 can comprise the diverse location for fluorocarbons cold-producing medium quencher in other parts of the arbitrary number that Fig. 7 does not show or process, and this depends on the details of particular embodiment.Such as, the alternative refrigeration system of any number can also be used for preparing LNG 702 from natural gas stream 704.In addition, the different refrigeration system of any number can be combined to prepare LNG 702.
For system prepared by LNG
Fig. 8 A and 8B is the process chart of cascade cooling system 800.This cascade cooling system 800 may be used for the preparation of LNG, and can implement in hydrocarbon system of processing.This cascade cooling system 800 can operate at low temperatures, such as, lower than approximately-18 DEG C, or lower than approximately-29 DEG C, or lower than approximately-40 DEG C.In addition, this cascade cooling system 800 can use more than a kind of cold-producing medium and provide refrigeration at multiple temperature.
Cascade cooling system 800 can comprise the first fluorocarbons refrigeration system 802, and as shown in Figure 8 A, it can use the first fluorocarbons cold-producing medium, such as R-410A.Cascade cooling system 800 can also comprise the second fluorocarbons refrigeration system 804, and as shown in Figure 8 B, it can use the second fluorocarbons cold-producing medium, such as R-508B.In addition, cascade cooling system 800 can comprise nitrogen refrigeration system 806, as shown in Figure 8 B.
Natural gas stream 808 can flow through quencher 810, and it is pre-cooled natural gas stream 808 by the indirect heat exchange with cooling fluid.Can flow in the pipe joint 812 of cascade cooling system 800 after natural gas stream 808.This pipe joint 812 can be configured to natural gas stream 808 to be divided into three independent natural gas streams.First natural gas stream can be flowed in the first fluorocarbons refrigeration system 802 by pipeline 814, and the second natural gas stream and the 3rd natural gas stream can be flowed in the system with Fig. 9 relevant discussion respectively by pipeline 816 and 818.
Natural gas stream can flow in the first fluorocarbons refrigeration system 802 for cooled natural gas logistics in preparation.This natural gas stream can by cooling through a series of heat exchangers 820,822 and 824 in the first fluorocarbons refrigeration system 802.This heat exchanger 820,822 and 824 can also refer to evaporimeter, quencher or ice chest.Natural gas stream can by cooling in each in heat exchanger 820,822 and 824 of the indirect heat exchange with circulation fluorocarbons cold-producing medium.This fluorocarbons cold-producing medium can be HFC, such as R-410A or R-404A, or the fluorocarbons cold-producing medium of any other suitable type.
Fluorocarbons cold-producing medium can circulate continuously through the first fluorocarbons refrigeration system 802, and it can prepare fluorocarbons cold-producing medium to enter each in heat exchanger 820,822 and 824 by continuous print.Fluorocarbons cold-producing medium can flow out First Heat Exchanger 820 by pipeline 826 as steam fluorocarbons cold-producing medium.Steam fluorocarbons cold-producing medium can merge in two pipe joints 828 and 829 with other steam fluorocarbons cold-producing mediums.Then steam flows through compressor 830 to increase the pressure of steam fluorocarbons cold-producing medium, prepares overheated steam fluorocarbons cold-producing medium.Overheated steam fluorocarbons cold-producing medium flows through condenser 832, and it can cool and condensation superheated vapor fluorocarbons cold-producing medium, prepares liquid fluorocarbon compound cold-producing medium.
Liquid fluorocarbon compound cold-producing medium can flow through expansion valve 834, which reduces the temperature and pressure of liquid fluorocarbon compound cold-producing medium.This can cause the flash distillation of liquid fluorocarbon compound cold-producing medium, prepares the mixture of liquid fluorocarbon compound cold-producing medium and steam fluorocarbons cold-producing medium.Liquid fluorocarbon cold-producing medium and steam fluorocarbons cold-producing medium can flow into the first flash tank 836 by pipeline 838.In the first flash tank 836, liquid fluorocarbon compound cold-producing medium can be separated from steam fluorocarbons cold-producing medium.
Steam fluorocarbons cold-producing medium can flow to pipe joint 828 by pipeline 839 from the first flash tank 836.This liquid fluorocarbon compound cold-producing medium can in inflow line joint 840, and liquid fluorocarbon compound cold-producing medium can be divided into two independent liquid fluorocarbon compound refrigerant stream by it.A liquid fluorocarbon compound refrigerant stream can flow through First Heat Exchanger 820, partly or entirely flashes to steam, and gets back to pipe joint 828 place by pipeline 826.Other liquid fluorocarbon compound refrigerant stream can flow to the second flash tank 842 place by pipeline 844.Pipeline 844 also comprises expansion valve 846, its can regulates liquid fluorocarbons refrigerant stream to control the flowing that liquid fluorocarbon compound refrigerant stream enters the second flash tank 842.In expansion valve 846, the adjustment of liquid fluorocarbon compound refrigerant stream can cause the flash vaporization of liquid fluorocarbon compound refrigerant stream, thus prepares the mixture of steam and liquid fluorocarbon compound cold-producing medium.
Liquid fluorocarbon compound cold-producing medium can be separated with steam fluorocarbons cold-producing medium by the second flash tank 842.This steam fluorocarbons cold-producing medium can by pipeline 850 inflow line joint 848.The steam fluorocarbons cold-producing medium that this pipe joint 848 can merge steam fluorocarbons cold-producing medium and reclaim from the second heat exchanger 822.Can flow in another pipe joint 852 after this steam fluorocarbons cold-producing medium.The steam fluorocarbons cold-producing medium that this pipe joint 852 can merge steam fluorocarbons cold-producing medium and reclaim from the 3rd heat exchanger 824.The steam fluorocarbons cold-producing medium merged can pressurize and by pipeline 856 inflow line joint 829 to merge the steam from flash tank 836 and heat exchanger 820 in compressor 854.
Liquid fluorocarbon compound cold-producing medium can flow to pipe joint 858 from the second flash tank 842, and liquid fluorocarbon compound cold-producing medium can be divided into two independent liquid fluorocarbon compound refrigerant stream by it.A liquid fluorocarbon compound refrigerant stream can flow through the second heat exchanger 822 and get back to pipe joint 848 place by pipeline 860.Another liquid fluorocarbon compound refrigerant stream can flow through the 3rd heat exchanger 824 by pipeline 862.Pipeline 862 can also comprise expansion valve 864, and this expansion valve allows the flash distillation of liquid fluorocarbon compound refrigerant stream, and reduces the pressure and temperature of liquid fluorocarbon compound refrigerant stream thus, when it flows into the 3rd heat exchanger 824.Liquid fluorocarbon compound refrigerant stream from the 3rd heat exchanger 824 can be compressed and deliver to pipe joint 852 place by pipeline 868 in compressor 866.
In different embodiments, the fluorocarbons cold-producing medium of the second fluorocarbons refrigeration system 804 is pre-cooled in the first fluorocarbons refrigeration system 802.Such as, the fluorocarbons cold-producing medium of the second fluorocarbons cold-producing medium can be pre-cooled by flowing through First Heat Exchanger 820.This fluorocarbons cold-producing medium can be HFC, such as R-508B, or the fluorocarbons of any other suitable type.This fluorocarbons cold-producing medium can flow to First Heat Exchanger 820 by pipeline 870 from the second fluorocarbons refrigeration system 804.
In each in heat exchanger 820,822 and 824 of natural gas stream gradually after chilling, it just flows in the second fluorocarbons refrigeration system 804 by pipeline 874, as shown in Figure 8 B.Second fluorocarbons refrigeration system 804 can comprise the 4th heat exchanger 876 and the 5th heat exchanger 878, and it can use the further cooled natural gas logistics of fluorocarbons cold-producing medium.
Fluorocarbons cold-producing medium can be continuously circulated through the second refrigeration system 804, and it prepares fluorocarbons cold-producing medium for entering each in heat exchanger 876 and 878.This fluorocarbons cold-producing medium can as steam fluorocarbons refrigerant stream from the 4th heat exchanger 876 out.This steam fluorocarbons refrigerant stream can merge in pipe joint 880 with another steam fluorocarbons refrigerant stream, and can merge in another pipe joint 882 with another steam fluorocarbons refrigerant stream from the 5th heat exchanger 878.Then this steam fluorocarbons refrigerant stream can flow through compressor 884, and it can make the pressure of steam fluorocarbons refrigerant stream increase, and prepares overheated fluorocarbons refrigerant stream.Overheated fluorocarbons refrigerant stream can flow through pipe joint 886 and another compressor 888, and it can increase the pressure of overheated fluorocarbons refrigerant stream further.
Overheated fluorocarbons refrigerant stream can flow through gas cooler 890.This gas cooler 890 can cool overheated fluorocarbons refrigerant stream, the steam fluorocarbons refrigerant stream of preparation cooling.In some cases, if steam fluorocarbons refrigerant stream is lower than environment temperature, this steam fluorocarbons refrigerant stream can't flow through gas cooler 890.The First Heat Exchanger 820 in the first fluorocarbons refrigeration system 802 can be flow through by pipeline 870 after liquid fluorocarbon compound refrigerant stream.
Once fluorocarbons refrigerant stream is through First Heat Exchanger 820, this fluorocarbons refrigerant stream can enter the 3rd flash tank 892 in the second fluorocarbons refrigeration system 804 by pipeline 894.Pipeline 894 can comprise the expansion valve 896 controlling fluorocarbons refrigerant stream inflow the 3rd flash tank 892.This expansion valve 896 can reduce the temperature and pressure of fluorocarbons refrigerant stream, and this causes the flash vaporization of fluorocarbons refrigerant stream for steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream.
Steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream can flash distillation enter in the 3rd flash tank 892, and steam fluorocarbons refrigerant stream can be separated with liquid fluorocarbon compound refrigerant stream by it.This steam fluorocarbons refrigerant stream can pass through pipeline 898 inflow line joint 886.Liquid fluorocarbon compound refrigerant stream can flow into the 4th flash tank 904 by pipeline 906 from the 3rd flash tank 892.Pipeline 906 can comprise the expansion valve 908 controlling fluorocarbons refrigerant stream inflow the 4th flash tank 904.This expansion valve 908 can reduce the temperature and pressure of fluorocarbons refrigerant stream further, and this causes the flash vaporization of fluorocarbons refrigerant stream for steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream.
Liquid fluorocarbon compound refrigerant stream can be left to pipe joint 910 from the 4th flash tank 904, and liquid fluorocarbon compound refrigerant stream can be divided into two independent liquid fluorocarbon compound refrigerant stream by it.Liquid fluorocarbon compound refrigerant stream can flow through the 4th heat exchanger 876 and by pipeline 912 return line joint 880 place.Another liquid fluorocarbon compound refrigerant stream can flow through the 5th heat exchanger 878 by pipeline 914.Pipeline 914 can also comprise the expansion valve 916 controlling liquid fluorocarbon compound refrigerant stream inflow the 5th heat exchanger 878, such as, by allowing the flash distillation of fluorocarbons refrigerant stream, reducing temperature and producing steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream.Can pressurize in compressor 918 from the steam fluorocarbons refrigerant stream obtained of the 5th heat exchanger 878 and afterwards in inflow line joint 882 to recycle.
After natural gas stream is cooled by the indirect heat exchange with fluorocarbons refrigerant stream in heat exchanger 876 and 878, natural gas stream can flow into nitrogen refrigeration system 806 by pipeline 920.In different embodiments, the nitrogen gas refrigerant logistics of nitrogen refrigeration system 806 carries out precooling by each flowing through in heat exchanger 820,822,824 and 876.Nitrogen gas refrigerant logistics 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 be cooled by the indirect heat exchange with nitrogen gas refrigerant logistics in the 6th heat exchanger 922.Nitrogen gas refrigerant logistics can cycle through nitrogen refrigeration system 806 by continuous print, and it has prepared the nitrogen gas refrigerant logistics for entering the 6th heat exchanger 922.Nitrogen gas refrigerant can flow through the 6th heat exchanger 922 as two independent nitrogen gas refrigerant logistics.Nitrogen gas refrigerant logistics from the 6th heat exchanger 922 can merge in pipe joint 924.
The nitrogen gas refrigerant logistics merged can flow through the 7th heat exchanger 926 by pipeline 928.In the 7th heat exchanger 926, nitrogen gas refrigerant logistics can provide cooling to the high pressure nitrogen refrigerant stream flowed in the opposite direction.Nitrogen gas refrigerant logistics from the 7th heat exchanger 926 can be pressurizeed in the first compressor 930, cools in the first quencher 932, pressurizes in the second compressor 934, and cools in the second quencher 936.Can inflow line joint 938 after the high pressure nitrogen refrigerant stream obtained, high pressure nitrogen refrigerant stream can be divided into two independent high pressure nitrogen refrigerant stream by it.
A high pressure nitrogen refrigerant stream from pipe joint 938 can flow through heat exchanger 820,822,824 and 876 by pipeline 921.Once leave the 4th heat exchanger 876, nitrogen gas refrigerant logistics can expand thus produce power in expander 940, and flows through the 6th heat exchanger 922 to provide the cooling to natural gas stream.
Another high pressure nitrogen refrigerant stream can flow through the 3rd compressor the 942, three quencher 944 and the 7th heat exchanger 926 from pipe joint 938.Can expand thus produce power in expander 946 after high pressure nitrogen refrigerant stream, and flow through the 6th heat exchanger 922 to provide cooling for natural gas stream.The energy produced in expander 940 and 946 is for generating electricity or driving all or some (part) in compressor 930,934 or 942.
Fig. 9 is the process chart of the system 900 comprising NRU 902.This system 900 can be positioned at the downstream of cascade cooling system 800, and can implement in the hydrocarbon system of processing identical with cascade cooling system 800.
Once natural gas stream cools in nitrogen refrigeration system 806, this natural gas stream can be just the form of LNG.This LNG logistics can flow into system 900 by pipeline 948.Especially, this LNG logistics can inflow line joint 950, and it can merge from the LNG logistics of pipeline 948 and the natural gas stream from pipeline 816.Initial cooling from the natural gas stream of pipeline 816 can be carried out before natural gas stream inflow line joint 950 in the 8th heat exchanger 952.
LNG logistics from pipe joint 950 can flow in NRU 902 to remove excessive nitrogen from LNG logistics.Especially, this LNG logistics can flow into reboiler 954, and it can reduce the temperature of LNG logistics.The LNG logistics of cooling can expand and flow through expansion valve 958 afterwards in hydraulic expansion turbine 956, which reduces the temperature and pressure of LNG logistics.
LNG logistics can flow into the low-temperature fractionation post 960 in NRU902, such as NRU tower.In addition, by pipeline 962, heat can be delivered to low-temperature fractionation post 960 from reboiler 954.Nitrogen can be separated by cryogenic distillation process by low-temperature fractionation post 960 from LNG logistics.Overhead stream can flow out low-temperature fractionation post 960 by pipeline 964.Overhead stream mainly can comprise methane, nitrogen and other low boilings or uncondensable gas, such as helium, and it separates from LNG system.
In some embodiments, overhead stream flows in evaporator overhead condenser (not shown), and it can be separated any liquid and make it turn back in low-temperature fractionation post 960 as backflow in overhead stream.This can cause a kind of steam stream, mainly comprise the fuel stream of methane and mainly comprise the preparation of another kind of steam stream of low-boiling point gas.Fuel stream can flow through the 8th heat exchanger 952 by pipeline 964.In the 8th heat exchanger 952, the temperature of vapor fueled logistics can be raised by the indirect heat exchange with natural gas stream, produces vapor fueled logistics.This vapor fueled logistics can merge in pipe joint 966 with other vapor fueled logistics.Can cool in a series of compressor 968,970 and 972 and quencher 974,976,978 after the vapor fueled logistics merged.In pipe joint 980, the vapor fueled logistics obtained can merge with the natural gas stream from pipeline 818, and it can be the vapor fueled logistics from natural gas stream 808.Can as fuel 982 by pipeline 984 outflow system 900 after vapor fueled logistics.
In low-temperature fractionation post 960, the bottoms of preparation mainly comprises the LNG with trace nitrogen.This LNG logistics can be flowed in LNG tank 986 by pipeline 988.Pipeline 988 can comprise the valve 990 entering the flowing of LNG tank 986 for control LNG logistics.LNG tank 986 can store between any one section of LNG logistics.The boiling emergent gas produced in LNG tank 986 can flow to pipe joint 966 place by pipeline 992.Point place at any time, final LNG logistics 994 can use pump 998 to be transported to LNG tank 996 place for flowing to market.Can reclaim in cascade cooling system 800 final LNG logistics 944 being loaded into the other boiling escaping gas 999 produced in LNG tank 996 simultaneously.
Be understandable that the process chart of Fig. 8 A, 8B and Fig. 9 is not intended to illustrate that cascade cooling system 800 or system 900 comprise all constituents of Fig. 8 A, 8B or Fig. 9 display.In addition, cascade cooling system 800 or system 900 can comprise other parts of the arbitrary number that Fig. 8 A, 8B or Fig. 9 do not show respectively, and this depends on the details of particular embodiment.In different embodiments, heat exchanger 820,822,824,876,878 and 922 comprises the pipe of high convection rate type.The pipe of this high convection rate type can reduce equipment size and reduce the storage for providing the cold-producing medium of cooling in heat exchanger 820,822,824,876,878 and 922.In addition, any one in heat exchanger 820,822,824,876,878,922 or 926 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 and 976 is centrifugal type compressor.In order to reduce cold-producing medium to the loss in air, each compressor 830,854,866,888,884,918,930,934,942,968,972 and 976 can also comprise recovery or seal leak gas recovery system.
Figure 10 A and 10B is the process chart of another cascade cooling system 1000.This cascade cooling system 1000 can be the improvement version of the cascade cooling system 800 of Fig. 8 A and 8B.Similar numeric item is described according to the project relevant to Fig. 8 A and 8B.This cascade cooling system 1000 can be implemented in hydrocarbon system of processing.
Cascade cooling system 1000 can comprise the first fluorocarbons refrigeration system 1002, and as shown in Figure 10 A, it can use the first fluorocarbons cold-producing medium, such as R-410A.Cascade cooling system 1000 can also comprise the second fluorocarbons refrigeration system 1004, and as shown in Figure 10 B, it can use the second fluorocarbons cold-producing medium, such as R-508B.In addition, cascade cooling system 1000 can comprise nitrogen refrigeration system 1006, as shown in Figure 10 B.
The first fluorocarbons refrigeration system 1002 of Figure 10 A can be similar with the first fluorocarbons refrigeration system 802 of Fig. 8 A.But the first fluorocarbons refrigeration system 1002 of Figure 10 A can comprise the heat exchanger 822,824 that the second heat exchanger 1008 and the 3rd heat exchanger 1010 replace in the first fluorocarbons refrigeration system 802 of Fig. 8 A.
In the first fluorocarbons refrigeration system 1002, by the fluorocarbons cold-producing medium of the second fluorocarbons refrigeration system 1004 by flowing through heat exchanger 820,1008 and 1010 and respectively precooling, condensation and excessively cold.This fluorocarbons cold-producing medium can be HFC, such as R-508B, or the fluorocarbons of any other suitable type.This fluorocarbons cold-producing medium can to flow to the heat exchanger 820,1008 and 1010 the first fluorocarbons refrigeration system 1002 from the second fluorocarbons refrigeration system 1004 by pipeline 870.Thus, the first fluorocarbons refrigeration system 1002 of Figure 10 A can provide the first fluorocarbons refrigeration system 802 precooling greatly than Fig. 8 A and the compression less to the second fluorocarbons cold-producing medium, because this fluorocarbons cold-producing medium flows through whole three heat exchangers 802,1008 and 1010.
Natural gas stream heat exchanger 820,1008 and 1010 each in chilling step by step.The second fluorocarbons refrigeration system 1004 is flowed into by pipeline 874, as shown in Figure 10 B after the natural gas stream of chilling.Second fluorocarbons refrigeration system 1004 can comprise the 4th heat exchanger 876 and the 5th heat exchanger 1012, and it can use the further cooled natural gas logistics of fluorocarbons cold-producing medium.
Fluorocarbons cold-producing medium can cycle through the second refrigeration system 1004 by continuous print, its for the preparation of enter heat exchanger 876 and 1012 each in fluorocarbons cold-producing medium.Fluorocarbons cold-producing medium can leave the 4th heat exchanger 876 as steam fluorocarbons refrigerant stream.This steam fluorine carbon refrigerant stream can merge in pipe joint 880 with another steam fluorocarbons refrigerant stream, and can merge in pipe joint 882 with another steam fluorine carbon refrigerant stream from the 5th heat exchanger 1012.Can flow through compressor 884 after this steam fluorocarbons refrigerant stream, it can increase the pressure of steam fluorocarbons refrigerant stream.Then this steam can flow through the First Heat Exchanger 820 in the first fluorocarbons refrigeration system 1002 by pipeline 870.
Once fluorocarbons refrigerant stream is through heat exchanger 820,1008 and 1010, fluorocarbons refrigerant stream can enter the 3rd flash tank 1013 in the second fluorocarbons refrigeration system 1004 by pipeline 1014.Pipeline 1014 can comprise expansion valve 908, and it controls the flowing that fluorocarbons refrigerant stream enters the 3rd flash tank 1013.Expansion valve 908 can reduce the temperature and pressure of fluorocarbons refrigerant stream, and this causes the flash distillation of fluorocarbons refrigerant stream for steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream.
Steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream flash distillation can enter the 3rd flash tank 1013, and steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream can be separated by it.Steam fluorocarbons refrigerant stream can pass through pipeline 1016 inflow line joint 880.Liquid fluorocarbon compound refrigerant stream can flow to pipe joint 910 from the 3rd flash tank 1013, and liquid fluorocarbon compound refrigerant stream can be divided into two independent liquid fluorocarbon compound refrigerant stream by it.Liquid fluorocarbon compound refrigerant stream can flow through the 4th heat exchanger 876 and by pipeline 912 return line joint 880 place.Another liquid fluorocarbon compound refrigerant stream can flow through the 5th heat exchanger 1012 by pipeline 914.Pipeline 914 also can comprise expansion valve 916, which control liquid fluorocarbon compound refrigerant stream and flow into the 5th heat exchanger 1012, such as by allowing the flash distillation of fluorocarbons refrigerant stream, reducing temperature and producing steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream is carried out.Can compress in compressor 918 from the steam fluorocarbons refrigerant stream obtained of the 5th heat exchanger 1012 and afterwards in inflow line joint 882 to recycle.
After natural gas stream is cooled by the indirect heat exchange with fluorocarbons refrigerant stream in heat exchanger 876 and 878, this 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 by flowing through each and the precooling in heat exchanger 820,1008,1010,876 and 1012.Nitrogen gas refrigerant logistics can flow to heat exchanger 820,1008,1010,876 and 1012 by pipeline 921 from nitrogen refrigeration system 1006.
In nitrogen refrigeration system 1006, natural gas stream can be cooled by the indirect heat exchange with nitrogen gas refrigerant logistics in the 6th heat exchanger 1018.This nitrogen gas refrigerant logistics can cycle through nitrogen refrigeration system 1006 by continuous print, and it has prepared the nitrogen gas refrigerant logistics for entering the 6th heat exchanger 1018.
Nitrogen gas refrigerant logistics from the 6th heat exchanger 1018 can merge in pipe joint 1020 with another nitrogen gas refrigerant logistics.The nitrogen gas refrigerant logistics merged can flow through the 7th heat exchanger 926 by pipeline 928.In the 7th heat exchanger 926, nitrogen gas refrigerant logistics can provide cooling to the high pressure nitrogen refrigerant stream of rightabout flowing.Nitrogen gas refrigerant logistics from the 7th heat exchanger 926 can be compressed in the first compressor 930, cool in the first quencher 932, compress in the second compressor 934, cool in the second quencher 936, compress in the 3rd compressor 1022 and cool in the 3rd quencher 1024.Can inflow line joint 1026 after the high pressure nitrogen refrigerant stream obtained, high pressure nitrogen refrigerant stream can be divided into two independent high pressure nitrogen refrigerant stream by it.
A high pressure nitrogen refrigerant stream from pipe joint 1026 can flow through heat exchanger 820,1008,1010,876 and 1012 by pipeline 921.Once leave the 5th heat exchanger 1012, nitrogen gas refrigerant logistics can expand in expander 1028, produce power, and inflow line joint 1020 is to merge with the nitrogen gas refrigerant logistics leaving the 6th heat exchanger 1018.
Other high pressure nitrogen refrigerant stream can flow through the 7th heat exchanger 926 from pipe joint 1026.Can expand in expander 1030 after this high pressure nitrogen refrigerant stream, produce power, and flow through the 6th heat exchanger 1018 to provide cooling for natural gas stream.The energy produced in expander 1028 and 1030 may be used for the part generating electricity or drive compressor 930,934 or 1022.
Once natural gas stream cools in nitrogen cooling system 1006, natural gas stream can be the form of LNG.This LNG logistics can be flowed in the system 900 of Fig. 9 by pipeline 948.In system 900, nitrogen can remove from the LNG NRU 902, and as with Fig. 9 relevant discussion, finally can obtain LNG logistics 994.
Figure 10 C is the process chart of the selective embodiment of cascade cooling system 1000, and it has the nitrogen refrigeration system 1032 of simplification.As illustrated in figure 10 c, pipe joint 1020 and 1026, the 7th heat exchanger 926, expander 1030 and quencher 932 and 936 not included in nitrogen refrigeration system 1032.In addition, the first compressor 930 and the second compressor 934 merge into independent unit, i.e. compressor 1134.In these embodiments, whole nitrogen gas refrigerant logistics flows through heat exchanger 820,1008,1010,876 and 1012 by pipeline 921.Thus, these embodiments simplify the design of cascade cooling system 1000.The energy produced in expander 1028 is for generating electricity or driving the part of compressor 1022 or 1134.
Be understandable that the process chart of Figure 10 A, 10B and Figure 10 C is not intended to illustrate that cascade cooling system 1000 comprises all constituents of Figure 10 A, 10B and Figure 10 C display.In addition, cascade cooling system 1000 can comprise other parts of the arbitrary number that Figure 10 A, 10B and Figure 10 C does not show, and this depends on the details of particular embodiment.
Figure 11 A and 11B is the process chart of another cascade cooling system 1100.This cascade cooling system 1100 can be the improvement version of the cascade cooling system 800 and 1000 of Fig. 8 A, 8B, 10A, 10B and 10C respectively.Similar numeric item is described according to the project relevant to Fig. 8 A, 8B, 10A, 10B and 10C.Cascade cooling system 1100 can be implemented in hydrocarbon system of processing.
Cascade cooling system 1100 can comprise the first fluorocarbons refrigeration system 1102, and as shown in Figure 11 A, it can use the first fluorocarbons cold-producing medium, such as R-410A.This cascade cooling system 1100 can also comprise the second fluorocarbons refrigeration system 1104, and as shown in Figure 11 B, it can use the second fluorocarbons cold-producing medium, such as R-508B.
Figure 11 C is the process chart from refrigeration system 1105 implemented in the hydrocarbon system of processing identical with the cascade cooling system 1100 of Figure 11 A with 11B.Similar numeric item according to Fig. 8 A, 8B, 9, project that 10A, 10B, 10C, 11A and 11B are relevant is described.May be used for preparing LNG from natural gas stream from refrigeration system 1105.In addition, the NRU 1106 for removing nitrogen from natural gas stream can be comprised from refrigeration system 1105.
Natural gas stream 808 can flow through quencher 810, and it is by making natural gas stream 808 precooling with the indirect heat exchange of cooling fluid.Then this natural gas stream 808 flows into the pipe joint 812 in cascade cooling system 1100.Pipe joint 812 can be configured to natural gas stream 808 to be divided into three independently natural gas streams.First natural gas stream can pass through pipeline 814 inflow line joint 1107, and the second natural gas stream and the 3rd natural gas stream can flow into from refrigeration system 1105 respectively by pipeline 816 and 818.
In pipe joint 1107, natural gas stream can merge from the methane recirculation stream returned from refrigeration system 1105 with by pipeline 1108.Can flow into after the natural gas stream merged in the first fluorocarbons refrigeration system 1102 for the preparation of natural gas stream cooling.This natural gas stream can by cooling through a series of heat exchangers 1110,822 and 824 in the first fluorocarbons refrigeration system 1102.This natural gas stream can be cooled by the indirect heat exchange of the fluorocarbons cold-producing medium with circulation in each of heat exchanger 1110,822 and 824, as relevant Fig. 8 A discusses.
Then the natural gas stream cooled flows in the second fluorocarbons refrigeration system 1104 by pipeline 874, as shown in Figure 11 B.Second fluorocarbons refrigeration system 1104 can comprise the 4th heat exchanger 1112 and the 5th heat exchanger 1114, and it can use fluorocarbons refrigerant cools natural gas stream further.
Fluorocarbons cold-producing medium can be continuously circulated through the second refrigeration system 1104, and it has prepared the fluorocarbons cold-producing medium of each for entering in heat exchanger 1112 and 1114.This fluorocarbons cold-producing medium can leave the 4th heat exchanger 1112 as steam fluorocarbons refrigerant stream.Steam fluorocarbons refrigerant stream can merge in pipe joint 880 with another steam fluorocarbons refrigerant stream, and can merge in pipe joint 882 with another steam fluorocarbons refrigerant stream from the 5th heat exchanger 1114.Flow through compressor 884 after this steam fluorocarbons refrigerant stream, it can increase the pressure of steam fluorocarbons refrigerant stream.Then this steam can flow through the First Heat Exchanger 1110 in the first fluorocarbons refrigeration system 1102 by pipeline 870.
Once fluorocarbons refrigerant stream is through heat exchanger 1110,822 and 824, this fluorocarbons refrigerant stream can enter the 3rd flash tank 1013 in the second fluorocarbons refrigeration system 1104 by pipeline 1014.Pipeline 1014 can comprise expansion valve 908, which control fluorocarbons refrigerant stream and flows into the 3rd flash tank 1013.Expansion valve 908 can reduce the temperature and pressure of fluorocarbons refrigerant stream, causes the flash distillation of fluorocarbons refrigerant stream for steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream.
Steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream can flash distillation enter in the 3rd flash tank 1013, and steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream can be separated by it.This steam fluorocarbons refrigerant stream can pass through pipeline 1016 inflow line joint 880.Liquid fluorocarbon compound refrigerant stream can flow to pipe joint 910 from the 3rd flash tank 1013, and liquid fluorocarbon compound refrigerant stream can be divided into two independently liquid fluorocarbon compound refrigerant stream by it.Liquid fluorocarbon compound refrigerant stream can flow through the 4th heat exchanger 1112 and by pipeline 912 return line joint 880 place.Another liquid fluorocarbon refrigerant stream can flow through the 5th heat exchanger 1114 by pipeline 914.Pipeline 914 can also comprise and controls the expansion valve 916 that liquid fluorocarbon compound refrigerant stream flows into the 5th heat exchanger 1114, such as by allowing the flash distillation of fluorocarbons refrigerant stream, reduce temperature and produce steam fluorocarbons refrigerant stream and liquid fluorocarbon compound refrigerant stream is carried out.The steam fluorocarbons refrigerant stream obtained from the 5th heat exchanger 1114 can compress in compressor 918 and afterwards inflow line joint 882 to recycle.
Natural gas stream is by after cooling with fluorocarbons refrigerant stream indirect heat exchange in heat exchanger 1112 and 1114, and natural gas stream can be flowed into from refrigeration system 1105 by pipeline 1116.More particularly, this natural gas stream can flow in the 6th heat exchanger 1118 of refrigeration system 1105.In the 6th heat exchanger 1118, this natural gas stream can be cooled by the natural gas stream indirect heat exchange of lower temperature that flows with rightabout.
Natural gas stream from the 6th heat exchanger 1118 can inflow line joint 1120, and natural gas stream is divided into two independent natural gas streams by it.A natural gas stream can flow through expansion valve 1122, and it can reduce the temperature and pressure of this natural gas stream.The 6th heat exchanger 1118 can be flowed into by pipeline 1124 after cryogenic natural gas logistics, and may be used for the natural gas stream in cooling the 6th heat exchanger 1118.Natural gas stream from the 6th heat exchanger 1118 can inflow line joint 1126, and wherein it can merge with another natural gas stream.The natural gas stream of this merging can compress and flow into afterwards in the pipe joint 1107 in the first fluorocarbons refrigeration system 1102 in compressor 1128.
Other natural gas streams from pipe joint 1120 can flow in other pipe joints 1130, and wherein it can merge with another natural gas stream.The natural gas stream merged can flow into NRU 1106 to remove excessive nitrogen from this natural gas stream.Especially, natural gas stream can flow in reboiler 954, and it can reduce the temperature of natural gas stream.The natural gas stream of cooling can expand and flow through expansion valve 988 afterwards in hydraulic expansion turbine 986, and this valve reduces the temperature and pressure of natural gas stream.
Natural gas stream can flow in the low-temperature fractionation post 960 in NRU 1106.In addition, heat can pass to low-temperature fractionation post 960 by pipeline 962 from reboiler 954.Nitrogen and natural gas stream can be separated by low temperature distillation process by this low-temperature fractionation post 960.Overhead stream can flow out low-temperature fractionation post 960 by pipeline 964.Overhead stream mainly can comprise methane, nitrogen and other low boilings or uncondensable gas, the helium such as separated from natural gas stream.
In some embodiments, overhead stream flows in evaporator overhead condenser 1132, and it can any liquid in separation top logistics and make it return in low-temperature fractionation post 960 as backflow by pipeline 1134.The fuel stream that this can cause preparing a kind of steam stream, mainly comprise methane and the another kind of steam stream mainly comprising low-boiling point gas.Fuel stream can flow through the 7th heat exchanger 1136 by pipeline 964.In the 7th heat exchanger 1136, the temperature of vapor fueled logistics can be raised by the indirect heat exchange with the natural gas stream from pipeline 816, prepares vapor fueled logistics.This vapor fueled logistics can be compressed and chilling in a series of compressor 1138 and 1140 and quencher 1142 and 1144.The vapor fueled logistics obtained can merge with the natural gas stream from pipeline 818 in pipe joint 980, and it can be the vapor fueled logistics from natural gas stream 808.Can be flowed out from refrigeration system 1105 as fuel 982 by pipeline 984 after this vapor fueled logistics.
In low-temperature fractionation post 960, the bottoms of preparation mainly comprises the LNG with trace nitrogen.This bottoms can flow through evaporator overhead condenser 1132 by pipeline 1146.Pipeline 1146 can also comprise the expansion valve 1148 controlling bottoms inflow evaporator overhead condenser 1132.This bottoms can be used as the cold-producing medium of evaporator overhead condenser 1132.
The mixed phase stream obtained from evaporator overhead condenser 1132 can flow into the first flash tank 1150 by pipeline 1152.Mixed phase stream can be divided into the steam stream mainly comprising natural gas and LNG logistics by this first flash tank 1150.This steam stream can in inflow line joint 1154.Pipe joint 1154 can make this steam stream and another steam stream reclaimed by the second flash tank 1156 merge.The steam stream merged can flow into compressor 1158 by pipeline 1160.Natural gas stream from compressor 1158 can in inflow line joint 1126.
LNG logistics from the first flash tank 1150 can flow into the second flash tank 1156 by pipeline 1162.Pipeline 1162 can comprise the expansion valve 1164 that control LNG logistics flows into the second flash tank 1156, and it allows a part of liquid flashes from LNG logistics, produces the mixed phase system of inflow second flash tank 1156.
Mixed phase stream can be separated into LNG and comprise the steam stream of natural gas by the second flash tank 1156.This steam stream can pass through pipeline 1168 inflow line joint 1166.Pipe joint 1166 can make steam stream merge with the another kind of steam stream reclaimed by the 3rd flash tank 1170.The steam stream of this merging can compress and in inflow line joint 1154 in compressor 1172.
Then LNG logistics is flowed in the 3rd flash tank 1170 by pipeline 1174.Pipeline 1174 can comprise the expansion valve 1176 that control LNG logistics flows into the 3rd flash tank 1170, and it allows a part from the liquid flashes of LNG.3rd flash tank 1170 can reduce the temperature and pressure of LNG logistics further to such an extent as to LNG logistics close to equilibrium temperature and pressure.The steam stream of preparation can inflow line joint 1178, and it can make steam stream merge with the boiling escaping gas reclaimed from LNG tank 1180.The steam stream merged can compress and in inflow line joint 1166 in compressor 1182.
LNG logistics can be flowed in LNG tank 1180 by pipeline 1184.This LNG tank 1180 can store LNG logistics a period of time.The boiling escaping gas produced in LNG tank 1180 can flow to pipe joint 1178 place by pipeline 1186.At any time, final LNG logistics 994 can use pump 998 to be transported in LNG tank 996, for being transported to market.Final LNG logistics 994 is loaded into other boiling escaping gas 999 simultaneously produced in LNG tank 946 to reclaim in cascade cooling system 1100.
Be understandable that Figure 11 A, 11B and 912 process chart be not intended to all constituents that cascade cooling system 1100 is described or comprises Figure 11 A, 11B or 11C display from refrigeration system 1105.In addition, cascade cooling system 1100 or can comprise other parts of the arbitrary number that Figure 11 A, 11B or 11C do not show from refrigeration system 1105 respectively, this depends on the details of particular embodiment.
Fig. 8 A and 8B; 10A, 10B and 10C; The pressure of the refrigerant stream in 11A and 11B cascade cooling system 800,1000 and 1100 separately can have significant change.In some embodiments, minimum refrigerant pressure is a little more than local atmospheric pressure, but it also can be vacuum.In other embodiments, minimum refrigerant pressure is between about 7-9ps ia.It reduce coolant temperature, improve the load of fluorocarbons refrigeration system, but be reduction of the load from refrigeration system of nitrogen refrigeration system or methane.In some embodiments, use subatmospheric pressure to allow refrigerant energy to move in different fluorocarbons refrigeration systems, allow the use of load balance and the exercisable driver of Geng Duo.Such as, in some cases, cold-producing medium driver can be identical for all fluorocarbons refrigeration systems and nitrogen refrigeration system.
Form the method for LNG
Figure 12 is the process chart of the method 1200 for forming LNG from natural gas stream.Method 1200 can be implemented in the hydrocarbon system of processing of any suitable type.Method 1200 starts at module 1202 place, cools in the first fluorocarbons refrigeration system at this place's natural gas stream.This first fluorocarbons refrigeration system can be mechanical refrigeration system, valve expansion system, turbine expansion system or similar system.First fluorocarbons refrigeration system uses the first fluorocarbons cold-producing medium so that cooled natural gas logistics.First fluorocarbons cold-producing medium can be such as hydrofluorocarbon refrigerants, such as R-410A, or the fluorine carbon cold-producing medium of any suitable type.
In different embodiments, the first fluorocarbons cold-producing medium providing compression is compressed to the first fluorocarbons cold-producing medium, and the first fluorocarbons cold-producing medium of compression is cooled by the indirect heat exchange with cooling fluid.First fluorocarbons cold-producing medium of compression can expand to cool the first fluorocarbons cold-producing medium of this compression, prepares the first fluorocarbons cold-producing medium that expand, cooling thus.This expansion, cooling the first fluorocarbons cold-producing medium can pass heat exchange area, it can be the heat exchanger of any suitable type, such as quencher or evaporimeter.In addition, natural gas stream can by carrying out compressing and cooling with the indirect heat exchange of external refrigeration fluid.Then this natural gas stream can use the first fluorocarbons cold-producing medium chilling that expand, cooling in heat exchange area.
First fluorocarbons refrigeration system can also comprise the extra cooling stages of any number for cooled natural gas logistics.Such as, the first fluorocarbons refrigeration system can be three stage refrigeration systems, and it comprises three heat exchange area for by with the first fluorocarbons cold-producing medium indirect heat exchange and cooled natural gas.
In module 1204, natural gas stream cools 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 uses the second fluorocarbons cold-producing medium so that cooled natural gas logistics.Second fluorocarbons cold-producing medium can be such as hydrofluorocarbon refrigerants, such as R-508B, or the fluorocarbons cold-producing medium of any other suitable type.
In different embodiments, the second fluorocarbons cold-producing medium providing compression is compressed to the second fluorocarbons cold-producing medium, and the second fluorocarbons cold-producing medium of compression is by cooling with the indirect heat exchange of cooling fluid.Second fluorocarbons cold-producing medium of compression can expand to cool the second fluorocarbons cold-producing medium of this compression, prepares the second fluorocarbons cold-producing medium that expand, cooling thus.This expansion, cooling the second fluorocarbons cold-producing medium can pass heat exchange area, it can be the heat exchanger of any suitable type, such as quencher or evaporimeter.In addition, natural gas stream can by carrying out compressing and cooling with external refrigeration fluid indirect heat exchange.Then this natural gas stream can use the second fluorocarbons cold-producing medium chilling that expand, cooling in heat exchange area.
Second fluorocarbons refrigeration system can also comprise the extra cooling stages of any number for cooled natural gas logistics.Such as, the second fluorocarbons refrigeration system can be two benches refrigeration system, and it comprises two heat exchange area for by with the second fluorocarbons cold-producing medium indirect heat exchange and cooled natural gas.In addition, the second fluorocarbons cold-producing medium can precooling in the first fluorocarbons refrigeration system.Such as this can implement by making the heat exchange area that the second fluorocarbons cold-producing medium flows through in the first fluorocarbons refrigeration system.
In module 1206, by natural gas stream liquefaction to form LNG in nitrogen refrigeration system.Nitrogen gas refrigerant may be used for liquefied natural gas in nitrogen refrigeration system.This 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, expands so that produce power and reduce the temperature of nitrogen gas refrigerant, and flow through heat exchanger in hydraulic expansion turbine.In heat exchanger, natural gas stream liquefaction can be crossed and natural gas stream indirect heat exchange and prepare LNG with accommodation by nitrogen gas refrigerant.
In module 1208, in NRU, from LNG, remove nitrogen.NRU can comprise low-temperature fractionation post, such as NRU tower.The nitrogen separated from LNG can flow out low-temperature fractionation post as overhead stream, and LNG can flow out low-temperature fractionation post as bottoms.In addition, may be used for providing cooling to the reflux condenser at nitrogen deliverying unit top from the liquid material bottom nitrogen deliverying unit.
Should be understood that the process chart of Figure 12 is not intended to the step of illustration method 1200 according to any specific order execution, or explanation all comprises all steps in often kind of situation.In addition, the extra step of any number also can be included in method 1200, and this depends on the details of particular embodiment.
Figure 13 is the process chart of the another kind of method 1300 for being formed LNG by natural gas stream.Similar numeric item is described according to the project relevant to Figure 12.Method 1300 can be implemented in the hydrocarbon system of processing of any suitable type.Method 1300 is included in cooled natural gas in the first fluorocarbons refrigeration system at module 1202 place, and in the second fluorocarbons refrigeration system at module 1204 place cooled natural gas.
In addition, in module 1302, by natural gas stream cooling to form LNG at methane in refrigeration system.This methane can comprise multiple expansion valve and flash tank for cooled natural gas from refrigeration system.In some embodiments, methane from refrigeration system be relevant Figure 11 C discuss from refrigeration system 1105.In addition, in some embodiments, nitrogen deliverying unit is positioned at the upstream of methane from refrigeration system.
Should be understood that the step that the process chart of Figure 13 is intended to illustration method 1300 can be carried out according to any special order, or all steps can be included in often kind of situation.In addition, any amount of additional step can be included in method 1300, and this depends on the details of particular embodiment.
Summary of drawings
The advantage of the technology of the present invention can better be understood 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 of the two benches refrigeration system comprising saveall;
Fig. 3 be comprise heat exchanger saveall single phase refrigeration system process chart;
Fig. 4 is the process chart of the cascade cooling system comprising 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 system;
Fig. 8 A and 8B is the process chart of the cascade fluorocarbons cooling system with nitrogen refrigeration;
Fig. 9 is the process chart of the system comprising NRU;
Figure 10 A and 10B is that another has the process chart of the cascade fluorocarbons cooling system of nitrogen refrigeration;
Figure 10 C is the process chart of a selective embodiment of the cascade fluorocarbons cooling system having nitrogen refrigeration cooling system and simplify nitrogen refrigeration system;
Figure 11 A and 11B is the process chart of another cascade cooling system;
Figure 11 C is the process chart from refrigeration system implemented in the hydrocarbon system of processing identical with the cascade cooling system of Figure 11 A with 11B;
Figure 12 is by the process chart of the method for natural gas adsorption LNG; And
Figure 13 is by the process chart of the another kind of method of natural gas adsorption LNG.
Detailed Description Of The Invention
The specific embodiments of the technology of the present invention is described in following detailed description part.But from the particular embodiment of following description for the technology of the present invention and the aspect of specific use, it is only intended to exemplary object and generally provides the description of exemplary.Therefore, this technology be not limited to the present invention describe specific embodiments, but comprise fall into appended claims book spirit and scope in all alternative, improved form and the equivalent form of value.
First, for the item of reference, some term for the application sets with for the context of the invention is the same with their implication.For situation about not defining in the present invention for term of the present invention, should provide according to the publication of at least one printing or the patent of publication the definition that those skilled in the art in the related art reflected give the most broad sense of this term.In addition, the technology of the present invention by this term in the present invention shown in the restriction of usage, its all equivalent form of value, synonym, new development and all think that it is in the scope of claims of the present invention for the term of same or similar object or technology.
Just as used in the present invention, " from refrigeration " refers to the method for a part of product stream for object of freezing.This by implementing based on providing the object of refrigeration capacity to extract a part of product stream before final cooling.The logistics of this extraction expands in valve or expander, and as the result expanded, the temperature of logistics declines.This logistics is used for the product stream in cooling heat exchanger.After heat exchange, this logistics second compression and blended with feed gas stream again.This method is also known as open cycle refrigeration.
Alternatively, " from refrigeration " refers to the method that liquid cools thus by reducing pressure.When liquid, make by oneself and coldly refer to by evaporative cooling liquid, it corresponds to the reduction of pressure.More particularly, when the liquid of a part is in the reduction through experience pressure while throttling arrangement, the liquid flashes of this part is steam.As a result, steam and residual liquid are both cooled to the saturation temperature under the pressure reduced.Such as, according to the embodiment that the present invention describes, can being undertaken so that natural gas cools along with the loss of heat during vaporizing by making natural gas remain on boiling point from refrigeration of natural gas.This method also refers to " flash distillation ".
Just as used in the present invention, " cascade cycle " refers to the system with two or more cold-producing mediums, and wherein cold second refrigerant is by the first warmer condensation of refrigerant.Therefore, a kind of cold-producing medium and another kind of " cascade " can get up by low temperature.Based on the pressure of stepped evaporation in saveall, often kind of cold-producing medium in cascade can have multiple chilling level.Compared with independent refrigeration system, it is favourable that cascade cycle is considered to for preparation LNG, because more can obtain lower temperature than independent refrigeration system in cascade cycle.
" compressor " or " coolant compressor " comprises any unit, device or the equipment that can increase refrigerant stream pressure.This comprises the coolant compressor with independent compression process or step, or has the coolant compressor of multistage compression or step, is more particularly the multistep coolant compressor in independent packaging or shell.The refrigerant stream of evaporation to be compressed can be supplied to coolant compressor with different pressure.Some stages of hydrocarbon cooling procedure or step can comprise two or more coolant compressors of parallel connection, series connection or both sides.The present invention is not by the type of coolant compressor, particularly any refrigerant loop or the restriction of arrangement or design.
Just as used in the present invention, " cooling " broadly refers to and makes the temperature of material and/or interior energy reduce and/or decline, such as any suitable amount.Cooling can comprise 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 the decline of similar temperature.Cooling can use any suitable radiator, such as steam generation, hot water heating, cooling water, air, cold-producing medium, other process-streams (integration) and their associating.One or more cooling sources can combine and/or cascade to reach the output temperature of expectation.Cooling step can use the cooling unit with any appropriate device and/or equipment.According to an embodiment, cooling can comprise indirect heat exchange, such as, have one or more heat exchanger.Heat exchanger can comprise any suitable design, such as shell-and-tube, brazed aluminum formula, Spiral wound and/or similar designs.In optionally scheme, cooling can use evaporation (heat of vaporization) to cool, and sensible heat cools, and/or direct heat transfer, such as by liquid Direct spraying in process-stream.
" cryogenic temperature " refers to the temperature of approximately-50 DEG C or lower.
Just as used in the present invention, term " dethanizer " and " domethanizing column " refer to the distillation column or destilling tower that may be used for component in the logistics of separating natural gas.Such as, domethanizing column is used for methane to be separated with heavy component with ethane with other volatile components.Methane fraction is typical in containing a small amount of inert gas, such as nitrogen, CO
2, or similar gas purified gases reclaim.
" fluorocarbons " also refers to " perfluorocarbon compound " or " PFC ", and it is the molecule comprising F and C atom.Fluorocarbons has F-C key, and depends on the number of carbon atom in species, C-C key.The example of fluorocarbons comprises perfluoroethane (C
2f
6)." HFC " or " HFC " is the fluorocarbons comprising H, F and C atom of specific type.HFC has H-C and F-C key, and depends on the number of carbon atom in species, C-C key.Some examples of HFC comprise fluoroform (CHF
3), pentafluoroethane (C
2hF
5), HFC-134a (C
2h
2f
4), heptafluoro-propane (C
3hF
7), HFC-236fa (C
3h
2f
6), pentafluoropropane (C
3h
3f
5) and tetrafluoropropane (C
3h
4f
4), in addition also have the compound of similar chemical constitution.
Term " gas " and " steam " exchange and use, and it is defined as the material of gaseous state or the mixture of material that distinguish with liquid or solid state.Same, term " liquid " represents the material of liquid condition or the mixture of material that distinguish with gas or solid state.
Any device that heat can be delivered to another kind of medium from a kind of medium of expression of " heat exchanger " broad sense, it comprises any special structure, such as, be commonly referred to as the device of heat exchanger.Heat exchanger comprises " direct heat exchanger " and " indirect heat exchanger ".Therefore, heat exchanger can be the known heat exchanger of shell-tubular type, spiral, hairpin formula, core type, core-autoclave, double hose, brazed aluminum formula, Spiral wound or any other type." heat exchanger " also refers to any post, tower, unit or other applicable one or more logistics that allow and extends therethrough, and carries out other layouts of direct or indirect heat exchange between one or more refrigeration lines and one or more feed streams.
" hydrocarbon " is the organic compound mainly comprising element hydrogen and carbon, although other elements of nitrogen, sulphur, oxygen, metal or any number also can exist on a small quantity.Just as used in the present invention, hydrocarbon is commonly referred to as the component found in natural gas, oil or chemical processing plant (CPP).
" liquefied natural gas " or " LNG " is usually the known natural gas comprising high percent-methane.But LNG can also comprise other compounds of trace.Other element or compound can include but not limited to ethane, propane, butane, carbon dioxide, nitrogen, helium, hydrogen sulfide or their associating, they are processed to remove one or more components (such as helium) or impurity (such as water and/or heavy hydrocarbon), and under almost atmospheric pressure, be condensed into liquid by cooling afterwards.
" liquefied petroleum gas " or " LPG " is commonly referred to as the mixture derived from the propane of refine crude oil, butane or other light hydrocarbons.At a normal temperature, LPG is gas.But LPG can cool or carry out pressurizeing to facilitate storing and transport.
" mixed refrigerant process " can include but not limited to the independent system using mix refrigerant, namely has the cold-producing medium more than a kind of chemical constituent, also comprises the mixed refrigerant systems of hydrocarbon precooling, and double-mixed refrigerant system.Usually, mix refrigerant comprises hydrocarbon and/or non-hydrocarbon component.Example typically for the suitable hydrocarbons component of mix refrigerant can include but not limited to methane, ethane, ethene, propane, propylene, butane and butylene isomer, and pentane.The non-hydrocarbon component be generally used in mix refrigerant can comprise nitrogen.Mixed refrigerant process uses at least one blending ingredients cold-producing medium, but also can additionally use one or more pure component refrigerants.
" natural gas " refers to the multicomponent gas obtained by crude oil well or aerogenesis rock stratum, underground.The composition of natural gas and pressure can be significantly different.Typical natural gas stream comprises methane (CH
4) as key component, be namely methane more than the natural gas stream of 50mol%.Natural gas stream can also comprise ethane (C
2h
6), hydrocarbon (the such as C of higher molecular weight
3-C
20hydrocarbon), one or more sour gas (such as carbon dioxide or hydrogen sulfide), or their any associating.Natural gas can also comprise a small amount of impurity, such as water, nitrogen, iron sulfide, wax, crude oil or their any associating.Owing to eliminating the compound serving as poisonous substance or solidify during cooling processing, to such an extent as to natural gas stream in for embodiment before can be in fact purifying.
Just as used in the present invention, " natural gas liquids " (NGL) refers to its component and such as typically weighs and the hydrocarbon mixture of condensation from natural gas than methane.Some examples of the hydrocarbon component of NGL logistics comprise ethane, propane, butane and pentane isomers, benzene, toluene and other aromatic compounds.
" nitrogen deliverying unit " or " NRU " refer to and are configured to receive natural gas feed stream and any system or the device of preparing net product logistics in fact, and this net product logistics is such as the methane stream being applicable to selling and the N comprising about 30% to 99%
2nitrogen stream.The example of NRU type comprises low temperature distillation, pressure-variable adsorption (PSA), UF membrane, Poor oil absorbing and solvent absorption.
" refrigerant component " in refrigeration system will absorb heat by evaporation at relatively low temperatures and pressures and discharge heat by under higher temperature and pressure by condensation.Illustrative refrigerant component can include but not limited to have the alkane of 1 to 5 carbon atoms, alkene and alkynes, nitrogen, chlorohydrocarbon, fluorohydrocarbon, other halogenated hydrocarbons, inert gas and their mixture or associating.
Refrigerant component generally includes one-component refrigerant.The one-component refrigerant with single halogenated hydrocarbons has relevant " R-" mark of two or three numerals, and it has reacted its chemical composition.This numeral adds 90 and gives and represent carbon, hydrogen and number of fluorine atoms object three numerals respectively.The first digit with three digital cold-producing mediums is unit lower than carbon number in molecule.If only containing a carbon atom in molecule, then omit first digit.Second digit is more than number of hydrogen atoms unit in molecule.Third digit equals the number of fluorine atoms in molecule.Unaccounted remaining key is occupied by chlorine atom.Suffix " a ", " b " or " c " of lowercase represent the asymmetry isomer increased.As special situation, R-400 series is made up of non-azeotrope blend, and R-500 series is made up of so-called azeotropic blend.Rightmost numeral is by any assignment of ASHRAE, and it is industrial organization.
When " in fact " is used in reference to the special characteristic of amount of substance or quantity or its, represents and be enough to provide the quantity of wishing the effect that this material or characteristic provide.The practical extent departed from can be allowed to depend on special context in some cases.
Embodiment
Embodiment of the present invention can comprise any associating of the method and system shown in following numbering paragraph.This does not think that it lists all possible embodiment completely, because the mode of texturing of any numbering can be expected to obtain by description of the invention.
1., for the formation of a hydrocarbon system of processing for liquefied natural gas (LNG), it comprises:
Be configured to the first fluorocarbons refrigeration system of use first fluorocarbons cold-producing medium chilling natural gas;
Be configured to the second fluorocarbons refrigeration system of the further chilling natural gas of use second fluorocarbons cold-producing medium;
Be configured to use nitrogen gas refrigerant cooled natural gas to prepare the nitrogen refrigeration system of LNG; And
Be configured to the nitrogen deliverying unit removing nitrogen from LNG.
2. the hydrocarbon system of processing of paragraph 1, wherein the first fluorocarbons refrigerant system configuration is the second fluorocarbons cold-producing medium of cooling second fluorocarbons 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 the two be configured to the nitrogen gas refrigerant of cool nitrogen refrigeration system.
4. the hydrocarbon system of processing of arbitrary section in paragraph 1-3, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system or the two comprise multiple cool cycles.
5. the hydrocarbon system of processing of arbitrary section in paragraph 1-4, wherein nitrogen refrigeration system comprises multiple being configured to and allows by the indirect heat exchange between natural gas and nitrogen gas refrigerant the heat exchanger of cooled natural gas.
6. the hydrocarbon system of processing of arbitrary section in paragraph 1-5, wherein the first fluorocarbons refrigeration system comprises:
Be configured to compression first fluorocarbons cold-producing medium to provide the compressor of the first fluorocarbons cold-producing medium of compression;
Be configured to pass the quencher cooling the first fluorocarbons cold-producing medium of this compression with the indirect heat exchange of cooling fluid;
Be configured to make the first fluorocarbons cold-producing medium of compression to expand to cool the valve of the first fluorocarbons cold-producing medium of this compression, prepare the first fluorocarbons cold-producing medium of cooling thus; And
Be configured to pass with the indirect heat exchange of the first fluorocarbons cold-producing medium cooled and the heat exchanger of cooled natural gas.
7. the hydrocarbon system of processing of arbitrary section in paragraph 1-6, wherein the second fluorocarbons refrigeration system comprises:
Be configured to compression second fluorocarbons cold-producing medium to provide the compressor of the second fluorocarbons cold-producing medium of compression;
Be configured to pass the quencher cooling the second fluorocarbons cold-producing medium of this compression with the indirect heat exchange of cooling fluid;
Be configured to make the second fluorocarbons cold-producing medium of compression to expand to cool the valve of the second fluorocarbons cold-producing medium of this compression, prepare the second fluorocarbons cold-producing medium of cooling thus; And
Be configured to pass with the indirect heat exchange of the second fluorocarbons cold-producing medium cooled and the heat exchanger of cooled natural gas.
8. the hydrocarbon system of processing of arbitrary section in paragraph 1-7, wherein the first fluorocarbons cold-producing medium comprises R-410A.
9. the hydrocarbon system of processing of arbitrary section in paragraph 1-8, wherein the second fluorocarbons cold-producing medium comprises R-508B.
10. the hydrocarbon system of processing of arbitrary section in paragraph 1-9, wherein the first fluorocarbons cold-producing medium or the second fluorocarbons cold-producing medium, or the two comprises non-toxic, non-combustible cold-producing medium.
The hydrocarbon system of processing of arbitrary section in 11. paragraph 1-10, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system, or the two comprises two or more quenchers and two or more compressors.
The hydrocarbon system of processing of arbitrary section in 12. paragraph 1-11, wherein the first fluorocarbons refrigeration system and the series connection of the second fluorocarbons refrigeration system are implemented.
The hydrocarbon system of processing of arbitrary section in 13. paragraph 1-12, wherein nitrogen gas refrigerant is gas phase.
The hydrocarbon system of processing of arbitrary section in 14. paragraph 1-13, wherein nitrogen refrigeration system comprises two or more quenchers, two or more expanders and two or more compressors.
The hydrocarbon system of processing of arbitrary section in 15. paragraph 1-14, wherein this hydrocarbon system of processing is configured to chilling for carrying out the natural gas of hydrocarbon dew point control.
The hydrocarbon system of processing of arbitrary section in 16. paragraph 1-15, wherein this hydrocarbon system of processing is configured to the natural gas that chilling extracts for natural gas liquids.
The hydrocarbon system of processing of arbitrary section in 17. paragraph 1-16, wherein this hydrocarbon system of processing is configured to methane to be separated with heavy gas with carbon dioxide with light gas.
The hydrocarbon system of processing of arbitrary section in 18. paragraph 1-17, wherein this hydrocarbon system of processing is configured to produce for the preparation of liquefied petroleum gas the hydrocarbon stored.
The hydrocarbon system of processing of arbitrary section in 19. paragraph 1-18, wherein this hydrocarbon system of processing is configured to condensing reflux logistics.
The method of 20. 1 kinds of formation liquefied natural gas (LNG), it comprises:
Cooled natural gas in the first fluorocarbons refrigeration system;
Cooled natural gas in the second fluorocarbons refrigeration system;
In nitrogen refrigeration system, liquefied natural gas is to form LNG; And
From LNG, nitrogen is removed in nitrogen deliverying unit.
The method of 21. paragraphs 20, it is included in the first fluorocarbons refrigeration system the second fluorocarbons cold-producing medium cooling the second fluorocarbons refrigeration system.
The method of 22. paragraphs 20 or 21, it is included in the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system, or in the two the nitrogen gas refrigerant of cool nitrogen refrigeration system.
The method of arbitrary section in 23. paragraph 20-22, wherein in the first fluorocarbons refrigeration system, cooled natural gas comprises:
Compress the first fluorocarbons cold-producing medium to provide the first fluorocarbons cold-producing medium of compression;
The first fluorocarbons cold-producing medium of this compression is cooled optionally through the indirect heat exchange with cooling fluid;
First fluorocarbons cold-producing medium of compression is expanded so that the first fluorocarbons cold-producing medium of cooled compressed, prepares the first fluorocarbons cold-producing medium of expansion, cooling thus;
Make described expansion, cooling the first fluorocarbons cold-producing medium by the first heat exchange area;
Optional compressed natural gas;
The cooled natural gas optionally through the indirect heat exchange with external refrigeration fluid; And
Make the first fluorocarbons refrigerant heat exchanger of natural gas and expansion, cooling.
The method of arbitrary section in 24. paragraph 20-23, wherein in the second fluorocarbons refrigeration system, cooled natural gas comprises:
Compress the second fluorocarbons cold-producing medium to provide the second fluorocarbons cold-producing medium of compression;
The second fluorocarbons cold-producing medium of this compression is cooled optionally through the indirect heat exchange with cooling fluid;
Second fluorocarbons cold-producing medium of compression is expanded so that the second fluorocarbons cold-producing medium of cooled compressed, prepares the second fluorocarbons cold-producing medium of expansion, cooling thus;
Make described expansion, cooling the second fluorocarbons cold-producing medium by the first heat exchange area;
Optional compressed natural gas;
The cooled natural gas optionally through the indirect heat exchange with external refrigeration fluid; And
Make the second fluorocarbons refrigerant heat exchanger of natural gas and expansion, cooling.
The method of arbitrary section in 25. paragraph 20-24, it comprises and uses one or more expansion turbine to make the nitrogen gas refrigerant of nitrogen refrigeration system remain gas phase.
The method of arbitrary section in 26. paragraph 20-25, it is included in the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system, or in the two, use two or more cooling stages chilling natural gases.
The method of arbitrary section in 27. paragraph 20-26, it is included in nitrogen refrigeration system and uses one or more cooling stages liquefied natural gas.
The method of arbitrary section in 28. paragraph 20-27, it comprises and uses heat exchanger to cool the first fluorocarbons cold-producing medium of the first fluorocarbons refrigeration system or the second fluorocarbons cold-producing medium of the second fluorocarbons refrigeration system, or both cooling.
The method of arbitrary section in 29. paragraph 20-28, it comprises the nitrogen gas refrigerant using heat exchanger cool nitrogen refrigeration system.
30. 1 kinds of hydrocarbon systems of processing for the formation of liquefied natural gas (LNG), it comprises:
Be configured to the first refrigeration system of use first fluorocarbons refrigerant cools natural gas, wherein this first refrigeration system comprise multiple be configured to allow by the indirect heat exchange between natural gas and the first fluorocarbons cold-producing medium the First Heat Exchanger of cooled natural gas
Be configured to the second refrigeration system of use second fluorocarbons cold-producing medium chilling natural gas, wherein this second refrigeration system comprise multiple be configured to allow by the indirect heat exchange between natural gas and the second fluorocarbons cold-producing medium the second heat exchanger of cooled natural gas;
Be configured to use nitrogen gas refrigerant by the 3rd refrigeration system of natural gas adsorption LNG, wherein the 3rd refrigeration system comprises multiple being configured to and allows by the indirect heat exchange between natural gas and nitrogen gas refrigerant the 3rd heat exchanger of cooled natural gas; And
Be configured to the nitrogen deliverying unit removing nitrogen from LNG.
The hydrocarbon system of processing of 31. paragraphs 30, wherein nitrogen gas refrigerant is gas phase.
The hydrocarbon system of processing of 32. paragraphs 30 or 31, wherein multiple First Heat Exchanger comprises being configured to pass and evaporates the first fluorocarbons cold-producing medium at least partly with the evaporimeter of cooled natural gas from natural gas to the heat trnasfer of the first fluorocarbons cold-producing medium.
The hydrocarbon system of processing of 33. paragraph 30-32, wherein multiple second heat exchanger comprises being configured to pass and evaporates the second fluorocarbons cold-producing medium at least partly with the evaporimeter of chilling natural gas from natural gas to the heat trnasfer of the second fluorocarbons cold-producing medium.
34. 1 kinds of hydrocarbon systems of processing for the formation of liquefied natural gas (LNG), it comprises:
Be configured to the first fluorocarbons refrigeration system of use first fluorocarbons cold-producing medium chilling natural gas;
Be configured to the second fluorocarbons refrigeration system of the further chilling natural gas of use second fluorocarbons cold-producing medium; And
Be configured to cooled natural gas to prepare the methane of LNG from refrigeration system.
The hydrocarbon system of processing of 35. paragraphs 34, it comprises the nitrogen deliverying unit of methane from refrigeration system upstream.
The hydrocarbon system of processing of 36. paragraphs 34 or 35, wherein methane comprises multiple expansion valve and multiple flash tank from refrigeration system.
Although technology of the present invention can allow to improve and replacement form, the embodiment discussed in the present invention is shown by means of only the mode of embodiment.But what should again understand is that these technology are not intended to be restricted to special embodiment disclosed by the invention.In fact, technology of the present invention comprise all fall into appended claims of the present invention true spirit and scope in alternative, improved form and the equivalent form of value.
Claims (33)
1., for the formation of a hydrocarbon system of processing for liquefied natural gas (LNG), it comprises:
Be configured to the first fluorocarbons refrigeration system of use first fluorocarbons cold-producing medium chilling natural gas;
Be configured to the second fluorocarbons refrigeration system of the further chilling natural gas of use second fluorocarbons cold-producing medium;
Be configured to use nitrogen gas refrigerant cooled natural gas to prepare the nitrogen refrigeration system of LNG; And
Be configured to the nitrogen deliverying unit removing nitrogen from LNG.
2. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigerant system configuration is the second fluorocarbons cold-producing medium of cooling second fluorocarbons refrigeration system.
3. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system or the two be configured to the nitrogen gas refrigerant of cool nitrogen refrigeration system.
4. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system or the two comprise multiple cool cycles.
5. the hydrocarbon system of processing of claim 1, wherein nitrogen refrigeration system comprise multiple be configured to allow by the indirect heat exchange between natural gas and nitrogen gas refrigerant the heat exchanger of cooled natural gas.
6. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons refrigeration system comprises:
Be configured to compression first fluorocarbons cold-producing medium to provide the compressor of the first fluorocarbons cold-producing medium of compression;
Be configured to pass the quencher cooling the first fluorocarbons cold-producing medium of this compression with the indirect heat exchange of cooling fluid;
Be configured to make the first fluorocarbons cold-producing medium of compression to expand to cool the valve of the first fluorocarbons cold-producing medium of this compression, prepare the first fluorocarbons cold-producing medium of cooling thus; And
Be configured to pass with the indirect heat exchange of the first fluorocarbons cold-producing medium cooled and the heat exchanger of cooled natural gas.
7. the hydrocarbon system of processing of claim 1, wherein the second fluorocarbons refrigeration system comprises:
Be configured to compression second fluorocarbons cold-producing medium to provide the compressor of the second fluorocarbons cold-producing medium of compression;
Be configured to pass the quencher cooling the second fluorocarbons cold-producing medium of this compression with the indirect heat exchange of cooling fluid;
Be configured to make the second fluorocarbons cold-producing medium of compression to expand to cool the valve of the second fluorocarbons cold-producing medium of this compression, prepare the second fluorocarbons cold-producing medium of cooling thus; And
Be configured to pass with the indirect heat exchange of the second fluorocarbons cold-producing medium cooled and the heat exchanger of cooled natural gas.
8. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons cold-producing medium comprises R-410A.
9. the hydrocarbon system of processing of claim 1, wherein the second fluorocarbons cold-producing medium comprises R-508B.
10. the hydrocarbon system of processing of claim 1, wherein the first fluorocarbons cold-producing medium or the second fluorocarbons cold-producing medium, or the two comprises non-toxic, non-combustible cold-producing medium.
The hydrocarbon system of processing of 11. claims 1, wherein the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system, or the two comprises 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 series connection of the second fluorocarbons refrigeration system are implemented.
The hydrocarbon system of processing of 13. claims 1, wherein nitrogen gas refrigerant is gas phase.
The hydrocarbon system of processing of 14. claims 1, wherein nitrogen refrigeration system comprises two or more quenchers, two or more expanders and two or more compressors.
The hydrocarbon system of processing of 15. claims 1, wherein this hydrocarbon system of processing is configured to chilling for carrying out the natural gas of hydrocarbon dew point control.
The hydrocarbon system of processing of 16. claims 1, wherein this hydrocarbon system of processing is configured to the natural gas that chilling extracts for natural gas liquids.
The hydrocarbon system of processing of 17. claims 1, wherein this hydrocarbon system of processing is configured to methane to be separated with heavy gas with carbon dioxide with light gas.
The hydrocarbon system of processing of 18. claims 1, wherein this hydrocarbon system of processing is configured to produce for the preparation of liquefied petroleum gas the hydrocarbon stored.
The hydrocarbon system of processing of 19. claims 1, wherein this hydrocarbon system of processing is configured to condensing reflux logistics.
The method of 20. 1 kinds of formation liquefied natural gas (LNG), it comprises:
Cooled natural gas in the first fluorocarbons refrigeration system;
Cooled natural gas in the second fluorocarbons refrigeration system;
In nitrogen refrigeration system, liquefied natural gas is to form LNG; And
From LNG, nitrogen is removed in nitrogen deliverying unit.
The method of 21. claims 20, it is included in the first fluorocarbons refrigeration system the second fluorocarbons cold-producing medium cooling the second fluorocarbons refrigeration system.
The method of 22. claims 20, it is included in the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system, or in the two the nitrogen gas refrigerant of cool nitrogen refrigeration system.
The method of 23. claims 20, wherein in the first fluorocarbons refrigeration system, cooled natural gas comprises:
Compress the first fluorocarbons cold-producing medium to provide the first fluorocarbons cold-producing medium of compression;
The first fluorocarbons cold-producing medium of this compression is cooled optionally through the indirect heat exchange with cooling fluid;
First fluorocarbons cold-producing medium of compression is expanded so that the first fluorocarbons cold-producing medium of cooled compressed, prepares the first fluorocarbons cold-producing medium of expansion, cooling thus;
Make described expansion, cooling the first fluorocarbons cold-producing medium by the first heat exchange area;
Optional compressed natural gas;
The cooled natural gas optionally through the indirect heat exchange with external refrigeration fluid; And
Make the first fluorocarbons refrigerant heat exchanger of natural gas and expansion, cooling.
The method of 24. claims 20, wherein in the second fluorocarbons refrigeration system, cooled natural gas comprises:
Compress the second fluorocarbons cold-producing medium to provide the second fluorocarbons cold-producing medium of compression;
The second fluorocarbons cold-producing medium of this compression is cooled optionally through the indirect heat exchange with cooling fluid;
Second fluorocarbons cold-producing medium of compression is expanded so that the second fluorocarbons cold-producing medium of cooled compressed, prepares the second fluorocarbons cold-producing medium of expansion, cooling thus;
Make described expansion, cooling the second fluorocarbons cold-producing medium by the first heat exchange area;
Optional compressed natural gas;
The cooled natural gas optionally through the indirect heat exchange with external refrigeration fluid; And
Make the second fluorocarbons refrigerant heat exchanger of natural gas and expansion, cooling.
The method of 25. claims 20, it comprises the one or more expansion turbine of use makes the nitrogen gas refrigerant of nitrogen refrigeration system remain gas phase.
The method of 26. claims 20, it is included in the first fluorocarbons refrigeration system or the second fluorocarbons refrigeration system, or in the two, use two or more cooling stages chilling natural gases.
The method of 27. claims 20, it is included in nitrogen refrigeration system and uses one or more cooling stages liquefied natural gas.
28. 1 kinds of hydrocarbon systems of processing for the formation of liquefied natural gas (LNG), it comprises:
Be configured to the first refrigeration system of use first fluorocarbons refrigerant cools natural gas, wherein this first refrigeration system comprise multiple be configured to allow by the indirect heat exchange between natural gas and the first fluorocarbons cold-producing medium the First Heat Exchanger of cooled natural gas
Be configured to the second refrigeration system of use second fluorocarbons cold-producing medium chilling natural gas, wherein this second refrigeration system comprise multiple be configured to allow by the indirect heat exchange between natural gas and the second fluorocarbons cold-producing medium the second heat exchanger of cooled natural gas;
Be configured to use nitrogen gas refrigerant by the 3rd refrigeration system of natural gas adsorption LNG, wherein the 3rd refrigeration system comprises multiple being configured to and allows by the indirect heat exchange between natural gas and nitrogen gas refrigerant the 3rd heat exchanger of cooled natural gas; And
Be configured to the nitrogen deliverying unit removing nitrogen from LNG.
The hydrocarbon system of processing of 29. claims 28, wherein nitrogen gas refrigerant is gas phase.
The hydrocarbon system of processing of 30. claims 28, wherein multiple First Heat Exchanger comprises being configured to pass and evaporates the first fluorocarbons cold-producing medium at least partly with the evaporimeter of cooled natural gas from natural gas to the heat trnasfer of the first fluorocarbons cold-producing medium.
The hydrocarbon system of processing of 31. claims 28, wherein multiple second heat exchanger comprises being configured to pass and evaporates the second fluorocarbons cold-producing medium at least partly with the evaporimeter of chilling natural gas from natural gas to the heat trnasfer of the second fluorocarbons cold-producing medium.
32. 1 kinds of hydrocarbon systems of processing for the formation of liquefied natural gas (LNG), it comprises:
Be configured to the first fluorocarbons refrigeration system of use first fluorocarbons cold-producing medium chilling natural gas;
Be configured to the second fluorocarbons refrigeration system of the further chilling natural gas of use second fluorocarbons cold-producing medium; And
Be configured to cooled natural gas to prepare the methane of LNG from refrigeration system.
The hydrocarbon system of processing of 33. claims 32, it comprises the nitrogen deliverying unit of methane from refrigeration system upstream, and wherein methane comprises multiple expansion valve and multiple flash tank from refrigeration system.
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2013
- 2013-11-01 MX MX2015005359A patent/MX2015005359A/en unknown
- 2013-11-01 IN IN3309DEN2015 patent/IN2015DN03309A/en unknown
- 2013-11-01 BR BR112015009964A patent/BR112015009964A2/en not_active IP Right Cessation
- 2013-11-01 JP JP2015543082A patent/JP6338589B2/en not_active Expired - Fee Related
- 2013-11-01 AU AU2013345176A patent/AU2013345176B2/en not_active Ceased
- 2013-11-01 CA CA2890089A patent/CA2890089C/en not_active Expired - Fee Related
- 2013-11-01 EP EP13855718.6A patent/EP2920532A4/en not_active Ceased
- 2013-11-01 WO PCT/US2013/067919 patent/WO2014078092A1/en active Application Filing
- 2013-11-01 CN CN201380059674.2A patent/CN104813127B/en not_active Expired - Fee Related
- 2013-11-01 SG SG11201503053SA patent/SG11201503053SA/en unknown
- 2013-11-01 US US14/437,168 patent/US20150285553A1/en not_active Abandoned
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2015
- 2015-04-23 CL CL2015001052A patent/CL2015001052A1/en unknown
- 2015-05-15 ZA ZA2015/03424A patent/ZA201503424B/en unknown
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106895662A (en) * | 2017-03-10 | 2017-06-27 | 蚌埠市荣强压缩机制造有限公司 | A kind of small-scaled natural gas liquification device |
| CN117109195A (en) * | 2023-10-19 | 2023-11-24 | 逸励柯环境科技(江苏)有限公司 | Transcritical carbon dioxide cold and hot combined supply unit |
| CN117109195B (en) * | 2023-10-19 | 2024-01-05 | 逸励柯环境科技(江苏)有限公司 | Transcritical carbon dioxide cold and hot combined supply unit |
Also Published As
| Publication number | Publication date |
|---|---|
| BR112015009964A2 (en) | 2017-07-11 |
| JP6338589B2 (en) | 2018-06-06 |
| MX2015005359A (en) | 2015-07-14 |
| SG11201503053SA (en) | 2015-06-29 |
| WO2014078092A1 (en) | 2014-05-22 |
| EP2920532A4 (en) | 2016-09-14 |
| CN104813127B (en) | 2017-05-31 |
| US20180172344A1 (en) | 2018-06-21 |
| US20150285553A1 (en) | 2015-10-08 |
| AU2013345176A1 (en) | 2015-06-04 |
| CA2890089C (en) | 2019-04-30 |
| EP2920532A1 (en) | 2015-09-23 |
| CL2015001052A1 (en) | 2015-11-20 |
| AU2013345176B2 (en) | 2016-12-22 |
| IN2015DN03309A (en) | 2015-10-09 |
| JP2016505793A (en) | 2016-02-25 |
| CA2890089A1 (en) | 2014-05-22 |
| ZA201503424B (en) | 2017-09-27 |
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