TWI314578B - Integrated ngl recovery and liquefied natural gas production - Google Patents
Integrated ngl recovery and liquefied natural gas production Download PDFInfo
- Publication number
- TWI314578B TWI314578B TW095117742A TW95117742A TWI314578B TW I314578 B TWI314578 B TW I314578B TW 095117742 A TW095117742 A TW 095117742A TW 95117742 A TW95117742 A TW 95117742A TW I314578 B TWI314578 B TW I314578B
- Authority
- TW
- Taiwan
- Prior art keywords
- stream
- reflux
- ethane
- rich
- scrubber
- Prior art date
Links
- 239000003949 liquefied natural gas Substances 0.000 title claims description 21
- 238000011084 recovery Methods 0.000 title description 5
- 238000010992 reflux Methods 0.000 claims description 135
- 239000007788 liquid Substances 0.000 claims description 100
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 96
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 85
- 238000000034 method Methods 0.000 claims description 69
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 claims description 54
- 230000002745 absorbent Effects 0.000 claims description 50
- 239000002250 absorbent Substances 0.000 claims description 50
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 40
- 238000001816 cooling Methods 0.000 claims description 22
- 150000002430 hydrocarbons Chemical class 0.000 claims description 20
- 238000009833 condensation Methods 0.000 claims description 19
- 230000005494 condensation Effects 0.000 claims description 19
- 229930195733 hydrocarbon Natural products 0.000 claims description 19
- 239000001294 propane Substances 0.000 claims description 19
- 238000010521 absorption reaction Methods 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 17
- 239000003345 natural gas Substances 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 11
- 238000005406 washing Methods 0.000 claims description 11
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 10
- 238000011144 upstream manufacturing Methods 0.000 claims description 10
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 9
- 239000005977 Ethylene Substances 0.000 claims description 9
- 238000005201 scrubbing Methods 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 7
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 6
- 239000001273 butane Substances 0.000 claims description 4
- 238000001354 calcination Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- VMGAPWLDMVPYIA-HIDZBRGKSA-N n'-amino-n-iminomethanimidamide Chemical compound N\N=C\N=N VMGAPWLDMVPYIA-HIDZBRGKSA-N 0.000 claims description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 4
- BOLDJAUMGUJJKM-LSDHHAIUSA-N renifolin D Natural products CC(=C)[C@@H]1Cc2c(O)c(O)ccc2[C@H]1CC(=O)c3ccc(O)cc3O BOLDJAUMGUJJKM-LSDHHAIUSA-N 0.000 claims description 4
- 239000006096 absorbing agent Substances 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims description 3
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 claims 3
- 238000009434 installation Methods 0.000 claims 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims 1
- 238000004140 cleaning Methods 0.000 claims 1
- 230000004048 modification Effects 0.000 description 11
- 238000012986 modification Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 238000005194 fractionation Methods 0.000 description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 description 2
- 239000001307 helium Substances 0.000 description 2
- 229910052734 helium Inorganic materials 0.000 description 2
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- BWGNESOTFCXPMA-UHFFFAOYSA-N Dihydrogen disulfide Chemical compound SS BWGNESOTFCXPMA-UHFFFAOYSA-N 0.000 description 1
- 101100516496 Drosophila melanogaster Pngl gene Proteins 0.000 description 1
- 206010036790 Productive cough Diseases 0.000 description 1
- 235000006040 Prunus persica var persica Nutrition 0.000 description 1
- 240000006413 Prunus persica var. persica Species 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- NLMBNVBBHYNBQY-UHFFFAOYSA-N [C].[Ru] Chemical class [C].[Ru] NLMBNVBBHYNBQY-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- RDHPKYGYEGBMSE-UHFFFAOYSA-N bromoethane Chemical compound CCBr RDHPKYGYEGBMSE-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- -1 carbonium compound Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 210000000078 claw Anatomy 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- WIZOZORCIQKFQD-UHFFFAOYSA-N ethane methane Chemical compound C.C.C.C.C.C.CC WIZOZORCIQKFQD-UHFFFAOYSA-N 0.000 description 1
- XLNZHTHIPQGEMX-UHFFFAOYSA-N ethane propane Chemical compound CCC.CCC.CC.CC XLNZHTHIPQGEMX-UHFFFAOYSA-N 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 1
- 125000001449 isopropyl group Chemical group [H]C([H])([H])C([H])(*)C([H])([H])[H] 0.000 description 1
- 210000004185 liver Anatomy 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
- 239000003921 oil Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 125000004817 pentamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 210000003802 sputum Anatomy 0.000 description 1
- 208000024794 sputum Diseases 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
- F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
- F25J1/0216—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle using a C3 pre-cooling cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
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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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
- F25J1/0241—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling wherein the overhead cooling comprises providing reflux for a fractionation step
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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
- F25J1/0258—Construction and layout of liquefaction equipments, e.g. valves, machines vertical layout of the equipments within in the cold box
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Description
,1314578 九、發明說明: 發明所屬之技術領域 天然氣主要包含甲烷及少許包括重質碳氫化合物的組 成成分。液化天然氣大部分都含有曱烷。比甲烷更重的後 氛化合物通常都以天然氣液體的形式凝縮並回收而產生有 價值的烴產物。 先前技術 - 典型的NG液化系統包含一洗滌塔,該洗滌塔以原料 天然氣或管線氣體供入並且產生富含曱烧的塔頂蒸氣及呈 '底部液體形式的NGL。一部分富含甲烷的塔頂蒸氣經局部 - 凝縮以提供用於該塔的迴流,而且其餘部分經液化以提供 該LNG產物。該底部液體經分餾而獲得個別的碳氫化合物 及/或呈有價值產物形式的烴餾分(部分)。 液化效率隨著提高壓力而改良,因此該NG液化壓力 • 應該要顯著地高於曱烷的臨界壓力以便使該LNG方法的能 i 4耗隶小化。然而,由該洗條塔回收重質碳氫化合物隨 著提高壓力而變得更困難’而且無法在高於其臨界壓力下 分離混合物。然而,該洗滌塔必須顯著地低於甲烷的臨界 • 壓力下操作以達到適當的分離。普通的解決方法在於使該 、 洗蘇塔供料膨脹然後壓縮該塔頂蒸氣。由該供料的等熵膨 服獲得的功可用於至少局部地驅動該塔頂壓縮機。此等解 決方法示於US-A-4-65278 (1977年,12月27日公開)中。 該洗滌塔供料膨脹之後接著該塔頂蒸氣的壓縮可藉著 5 、1314578 使從NGL分餾所獲得的重質成分呈吸收劑液體的形式再循 環至該洗條塔頂端或接近頂端而避免。舉例來說,
Chen-Hwa Chiu (油及氣體期刊,W97年,11月24日,第 56至63頁)記载以重質驗再循環物,例如所有或部分的q NGL部分,用於LNG方法的洗滌塔可提升經分離的混合物 之臨界壓力並且藉此提升該洗滌塔的操作壓力。有一例示 的方法中,從去丁烷器回收部分或全部的c4 NGL部分再循 環物。 W0 01101307/ US-A-2003 005 722/ US-B-6,74 2,3 5 8 (2002年12月2日/2003年1月9日/2004年6月1日公開) 揭示LNG方法,其中藉由凝縮從該塔中間位置抽取到的蒸 氣將頂部迴流供至该洗滌塔。其亦揭示分開地分顧經局部 凝縮的供料氣體的蒸氣及液體部分,並且來自該蒸氣部分 的分館之底部液體將中間或頂端迴流供至該液體部分的分 餾之方法。在所有的這些方法中,在液化之前先壓縮來自 該洗滌塔的蒸氣塔頂部分。 DE-A-10205366 (2003 年,8 月 21 日公開)揭示— 方法’其中冷卻來自該洗滌塔之富含乙烷的蒸氣塔頂部分 並且通至用於殘餘較高碳數碳氫化合物的移除之笛_ '、〜乐一·個 塔。以該第二個塔的底部液體將迴流供至該洗滌塔。較佳 地,以CU/C5 NGL部分將迴流供至該第二個塔。兮_ 口次一%的 精餾及吸附功能可結合於單一塔中。 US-A-6662589/ EP-A-1469266 (2003 年 12 月 16 2004年10月20日公開)揭示一 LNG方法,其中以包含比 6 s 1314578 乙烧更重的成分之NGL部分充當吸收劑液體供入該洗滌塔 的天然氣供入與富含甲烧的迴流物流供入之間的位置。在 該例示性具體例中,該迴流物流係藉由來自該洗滌塔塔頂 蒸氣的局部凝縮獲得。該洗滌塔塔頂部分在液化以提供該 LNG產物之前並未經壓縮。 W0 2004/010064 (2004 年 1 月 29 日公開)揭示一 lNC}
方法,其中C4/C5 NGL部分直接地或間接地供至該洗滌塔 以提供額外的迴流。該部分係供至該塔藉由該塔蒸氣塔頂 部分的局部凝縮所提供的供料處或上方。 該洗滌塔中的混合物臨界壓力也可利用富含乙烷的物 流迴流該塔而提高。這也能有良好的C2至c3分離及來自 NGL的高丙院(c3)回收率。 w〇-a-oi88447/us_a_6,401,486 (2〇〇1 年 u 月 日 / 2⑽2年6月u日公開)揭示_ lng方法其中用於該洗藤 塔的頂部迴流係由含有大部分甲烧及乙院與極少量丙燒的 蒸氣之凝縮提供。該洗料塔頂蒸氣全部都液化以提供該 ㈣產物’而且該洗滌塔底部物係於脱純化塔中分顧。 經凝縮以提供該頂部迴流的蒸氣可衍生自^ 田 ⑴纟自該NGL分顧的蒸氣塔頂部分及藉由閃館該經 二=佳地經低溫冷卻的洗梅塔塔頂部分至接近大氣壓 刀所獲传之視需要經閃餾的蒸氣; (11)該供料氣體部分的滑流; (出)藉由閃餾該經液化且輕 塔塔了I β ^ 5 μ 杈佳地Α低^冷郃的洗滌 P刀至接近大氣壓力所獲得之閃餾蒸氣; 7 .1314578 (iv)該錢化且較佳地㈣溫冷卻的洗糾塔頂部 分之一部分。 在選項⑴及㈣中’可藉由凝縮該供料氣體部分的滑 流而提供流至該洗滌塔的額外迴流,但沒有提供衍生自 NGL分餾及經區部凝縮的洗滌塔塔頂部分的迴流之教示。 在這些方法中,在液化之前並不需要壓縮該洗滌塔塔頂部 分。 EP-A-(H78207/ US_A_4,690,7〇2 〇986 年 4 月 15 日/ 1987 年 9 月 i 日公開);DE_A_38〇2553/ us_a_4,952,3〇5 (1989 年 8 月 3 日 / 1990 年 8 月 28 日公開);及 Ep_A_〇535;52/ US-A-5,291,736 (1993 年 4 月 7 日 / 1994 年 3 月 8 日公開) 全都揭示LNG方法,其中流至該洗滌塔的迴流係藉由凝縮 來自NGL分餾的蒸氣塔頂部分所獲得的甲烷與乙烷的混合 物而提供。這些專利之中任一顯示藉由局部地凝縮該塔頂 產物而獲得迴流。 已發現就熱力學效率、設備簡化及例如丙烷及丁烷等 有價值成分的觀點來自,該NGL及天然氣產物回收率可藉 著以有效的方式結合由局部地凝縮該洗滌塔塔頂部分所獲 知迴流的益處及富含乙烷與吸收劑液體的益處而得到改 善。 發明内容 在最廣義的形態中,本發明提供一種從曱烷在含乙燒 及更重的礙氫化合物之混合物中之供料回收比曱烷更重的 、1314578 成分之方法,該方法包含: 將該供料導入洗滌塔的第一個位置; 從該洗滌塔抽出比甲烷更重的成分中摒除的第一種仗 頂蒸氣流及富含比甲烷更重的成分之底部物流; 冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成第一 種二相物流; 分離該第一種二相物流以提供第二種塔頂蒸氣流及富 # 含甲燒的第一種迴流物流; 將該虽含曱烷的第一種迴流物流導入該洗滌塔第—個 位置上方的第二個位置; 將該底部物流分離成富含乙烷的物流及一或多種富含 * 比乙烷更重的成分之物流;以及 在選自第一個位置上方的第二個位置及第三個位置之 位置處,將衍生自該富含乙烷的物流之富含乙烷的第二種 迴流物流導入該洗滌塔。 ® 在本發明較佳的具體例中,使NGL分餾所獲得之富含 乙烷的物流,較佳地去乙烷器塔頂部分,凝縮,泵抽,結 合由局部地凝縮該洗滌塔塔頂蒸氣所獲得迴流物流並且再 循環至該洗滌塔,較佳地至洗滌塔的迴流筒。這使得該洗 , 滌塔能藉由提高該混合物的臨界壓力而在較高的壓力下操 - 作,同時能改善乙烷-丙烷分離。該富含乙烷的物流可使用 LNG方法主要熱交換器中可達到的混合冷凍劑(MR)冷凍作 用完全地凝縮而使該益處最大化。 重質再循環物流’特別是戊烷及異戊烷的使用,也有 9 1314578 益處。此物流可導至該迴流筒或直接地導至該洗滌塔。該 重質及輕質再循環物可單獨地結合並冷卻或,較佳地,與 凝縮該洗滌塔塔頂蒸氣所獲得的迴流物流混合。藉由凝縮 S亥塔頂療氣所獲得的迴流通常為流至該洗滌塔的全部迴流 (包括任何重質再循環物流)的約80%以上。在較佳的實施 方式中在主要LNG方法熱交換器的暖管束中進行冷卻。 實施方式 如上所述,本發明’以其最廣義的方法形態,提供一 種從曱烧在含乙烷及更重的碳氳化合物之混合物中之供料 回收比曱烧更重的成分之方法,該方法包含: 將該供料導入洗滌塔的第一個位置; 從該洗蘇塔抽出比甲烧更重的成分中摒除的第一種塔 頂蒸氣流及富含比曱烷更重的成分之底部物流; 冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成第一 種二相物流; 分離該第一種二相物流以提供第二種塔頂蒸氡流及富 含甲烧的第一種迴流物流; 將該富含曱烷的第一種迴流物流導入該洗滌塔第一個 位置上方的第二個位置; 將該底部物流分離成富含乙烷的物流及一或多種富含 比乙烷更重的成分之物流;以及 在選自第一個位置上方的第二個位置及第三個位置之 位置處’將衍生自該富含乙烷的物流之富含乙烷的第二種 10 1314578 迴流物流導入該洗滌塔。 在對應的裝置形態中,本發明提供一種藉由前述形態 的方法從甲烷在含乙烷及更重的碳氫化合物之混合物中之 供料回收比甲烷更重的成分之装置,該裝置包含: 一洗務塔; 用於將該供料導入洗膝塔第一個位置的的導管梦置· 用於從該洗滌塔抽出比曱烷更重的成分中摒除的第一 _ 種塔頂蒸氣流及昌含比甲烧更重的成分之底部物流的導管 裝置; 用於冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成 第一種二相物流的熱交換裝置; - 用於分離該第一種二相物流以提供第二種塔頂蒸氣流 及富含曱烧的第一種迴流物流的分離裝置; 用於將該富含曱烧的第一種迴流物流導入該洗條塔第 一個位置上方的第二個位置的導管裝置; 籲 用於將該底部物流分離成富含乙烷的物流及一或多種 虽含比乙烧更重的成分之物流的分離裝置;以及 用於選自第一個位置上方的第二個位置及第三個位置 之位置處,將衍生自該富含乙烷的物流之富含乙烷的第二 . 種迴流物流導入該洗滌塔的導管裝置。 . 在較佳的方法形態中’本發明提供一種從曱烷在含乙 烷及更重的碳氫化合物之混合物_之供料獲得液化甲烷之 方法,該方法包含: 將該供料導入洗務塔的第一個位置; -1314578 從該洗滌塔抽出比甲烷更重的成分中摒除的第~$塔 頂蒸氣流及富含比甲烷更重的成分之底部物流; 冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成第__ 種二相物流; 分離該第一種二相物流以提供第二種塔頂蒸氣流及富 含甲烷的第一種迴流物流; 液化該第二種塔頂蒸氣流; • 將該富含曱烷的第一種迴流物流導入該洗滌塔第一個 位置上方的第二個位置; 將該底部物流分離成富含乙烷的物流及一或多種富含 比乙烧更重的成分之物流;以及 ' 在選自第一個位置上方的第二個位置及第三個位置之 位置處,將衍生自該富含乙烷的物流之富含乙烷的第二種 迴流物流導入該洗滌塔。 在較佳的裝置形態中,本發明提供一種藉由根據該較 佳方法形態的方法從甲烷在含乙烷及更重的碳氫化合物之 ’匕s物中之供料獲得液化曱烧之裝置,該裝置包含: 一洗滌塔; 用於將该供料導入洗條塔第一個位置的的導管跋置· . 用於從該洗滌塔抽出比曱烷更重的成分中摒除的第— .:塔頂蒸氣流及富含比甲烷更重的成分之底部物流的導管 裝置; 用於冷卻並且局部土也凝縮該第一種塔頂蒸氣流而 一種二相物流的熱交換裝置; 12 1314578 用於分離該第一種二相物流以提供第二種塔頂蒸氣流 及富含曱烷的第一種迴流物流的分離裝置; 用於液化該第二種塔頂蒸氣流的熱交換裝置; 用於將該富含曱烷的第一種迴流物流導入該洗滌塔第 一個位置上方的第二個位置的導管裝置; 用於將該底部物流分離成富含乙烷的物流及一或多種 富含比乙烷更重的成分之物流的分離裝置;以及 用於選自第一個位置上方的第二個位置及第三個位置 之位置處,將衍生自該富含乙烷的物流之富含乙烷的第二 種迴流物流導入該洗滌塔的導管裝置。 如上所示,較佳地該供料為冷卻的天然氣供料並且液 化該第二種塔頂蒸氣以提供液化天然氣產物。 該富含乙烷的第二種迴流物流可與該富含曱烷的第一 種迴流物流分開地供入該洗滌塔,但較佳地使該富含乙烧 的第二種迴流物流在導入該洗滌塔之前先與該富含甲烷的 第一種迴流物流混合。該富含乙烷的物流在與該富含曱烷 的第一種迴流物流混合之前先局部地或完全地凝縮。該混 合宜在迴流筒的上游或其中進行,或藉著將該第一種二相 物流供至該富含乙烷的第二種迴流物流以迴流的形式供入 的吸收塔底部而進行。
該富含乙烷的物流,單獨或與一或多種其他加工流混 合之後,較佳地在低於導入該洗滌塔的供料溫度之溫度下 凝縮,並且在以富含乙烷的第二種迴流物流的形式導入該 洗滌塔之前先泵抽經凝縮的物流。該溫度通常為低於-32°F 13 1314578 (-35.5。。)。 通常,該富含乙烷的物流(130)係去乙烷器的蒸氣塔頂 部分。甲烧可從富含乙烧的物流移除,藉以該第二種迴流 物流基本上由乙烷組成。該第二種迴流物流含有少於約 0.05%的丙烷。 通常,該富含曱烷的第一種迴流物流構成全部迴流(亦 即供至該洗滌塔第一個位置上方的液體)的至少約8〇%,而 且該第二種迴流物流係少於全部迴流的約2〇%。 較佳地多於90%,特別是多於96%,的丙烷及/或丁烷 係以產物的形式從該底部物流回收得到。 如第6圖中舉例說明的,該第一種塔頂物流分兩階段 局部地凝縮,並且將來自各個凝縮的液體部分以迴流的形 式供至該洗條塔。 在較佳的具體例中,本發明的方法包含: 將該供料導入洗務塔的第一個位置; 從該洗滌塔抽出比甲烷更重的成分中摒除的第一種塔 頂蒸氣流及富含比甲烷更重的成分之底部物流; 冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成第— 種二相物流; 分離該第一種二相物流以提供第二種塔頂蒸氣流及富 含甲烷的第一種迴流物流; 田 將该虽含甲燒的第一種迴流物流導入該洗滌塔第—個 位置上方的第二個位置; 將該底部物流分離成富含乙烧的物流及二或多種富> 14 •1314578 比乙烧更重的成分之物流,該等物流包括富含比乙燒更重 的成分之吸收劑液體; 在選自第一個位置上方的第二個位置及第三個位置之 位置處’將衍生自該富含乙烷的物流之富含乙烷的第二種 迴流物流導入該洗滌塔;以及 在選自該洗滌塔第一個位置上方的第二個位置、第二 個位置及第四個位置之位置處,將該吸收劑液體導人該洗 滌塔。 在對應的較佳裝置具體例中,本發明的裝置包含: 一洗滌塔; 用於將該供料導入洗滌塔第一個位置的的導管裝置; 用於從該洗滌塔抽出比甲炫更重的成分中摒除的第— 種塔頂蒸氣流及富含比曱烷更重的成分之底部物流的導管 裝置; 用於冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成 第一種二相物流的熱交換裝置; 用於分離該第一種二相物流以提供第二種塔頂蒸氣流 及富含曱烷的第一種迴流物流的分離裝置; 用於將該富含甲烧的第一種迴流物流導入該洗蘇塔第 一個位置上方的第二個位置的導管裝置; 用於將該底部物流分離成富含乙烧的物流及二或多種 富含比乙烷更重的成分之物流,該等物流包括富含比乙烷 更重的成分之吸收劑液體,的分離裝置; 用於選自第一個位置上方的第二個位置及第三個位置 15 *1314578 之位置處’將衍生自該富含乙烷的物流之富含乙烷的第二 種迴流物流導入該洗膝塔的導管裝置;以及 用於選自該洗滌塔第一個位置上方的第二個位置、第 三個位置及第四個位置之位置處,將該吸收劑液體導入該 洗滌塔的導管裝置。 由以上討論的所有特徵與最廣義的形態關聯而應用於 此較佳具體例。 • 該吸收劑液體可包含C4碳氫化合物,但較佳地包含 C 5 +碳氫化合物。 該吸收劑液體可與該富含乙烷的第二種迴流物流或該 ' 富含甲烷的第一種迴流物流分開地供入該洗滌塔。然而, 較佳為S亥吸收劑液體在與導入該洗務塔之前先與該富含甲 院的第一種迴流物流及該富含乙烷的第二種迴流物流(i36) 其中至少一者結合。舉例來說’該吸收劑液體與該富含曱 燒的第一種迴流物流及該富含乙烧的第二種迴流物流其中 魯 至少一者在選自迴流筒的上游及其中之位置處結合,或可 將該第一種二相物流供至該吸收劑液體及視需要地該富含 乙烧的第二種迴流物流以迴流的形式供入的吸收塔底部。 該吸收劑液體可在該第一種塔頂蒸氣流局部凝縮之前先與 . 該第一種塔頂蒸氣流結合而形成第一種二相物流,及/或在 • 富含氣態乙烷的物流局部凝縮之前先與該富含氣態乙烷的 物流結合以提供第二種迴流物流。 可使結合的吸收劑液體與富含氣態乙烷的物流相分 離’並且將液體部分供至該洗滌塔第一個位置上方。該液 16 .1314578 體部分可在該第一種塔頂物流局部凝縮之前先與該第一種 塔頂物流結合以提供第一種二相物流。可使蒸氣部分凝縮 並且將凝縮的物流供至該洗滌塔第一個位置上方,在液化 之則加至該第二種塔頂蒸氣,或在該第一種塔頂物流局部 凝縮之前先與該第一種塔頂物流結合以提供第—種二相物 流。該經凝縮的蒸氣部分與該液體部分可在該第—種塔頂 物流局部凝縮之前先與該第一種塔頂物流結合以提供第一 ^ 種二相物流。 通常,該吸收劑液體將構成少於全部迴流(亦即供至該 洗滌塔第一個位置上方的液體)的約1〇%。 . 下文為僅藉由實施例及參照本發明現行較佳具體例的 . 附圖所做的說明。 參照第1圖’使含有主要地曱烷與。2至。6範圍的重 質碳氫化合物與極少量水、例如二氧化碳及二硫化氫等的 酸氣及例如水銀等的其他污染物之經預處理的加壓天然氣 • 供料uo在熱交換器112中冷卻至介於約—“卞卜“^與約 _40°F(-40°C)之間並且供至該洗滌塔114。典型地該供料ιι〇 係處理約600與約900磅/平方吋(4至6 25百萬帕)及約室 温下。熱交換器112表示藉著在不同壓下蒸發丙烧而冷卻 . 的多重階段。任何其他的冷卻手段,例如在單交換器中蒸 . 發混合的冷凍劑,都可使用。物流11〇’或該熱交換器u'2 下游的物流110之蒸氣部分可加以節流或等熵地膨脹至該 塔114中。由膨脹所獲得的能量可用於至少局部地壓縮另 一個物流,舉例來說加工流、12〇、15〇或156。 17 •1314578 洗滌塔114將該供料分離成富含重質碳氫化合物的底 部液體126及127及富含甲烷的「第一種」塔頂蒸氣流116。 在再沸器128中蒸發一部分127底部液體以供加熱該塔 114。該再沸器12 8可使用一部分供料物流丨丨〇,或任何其 他適合的加工流,以提供熱負荷(heat duty)。該塔也可具有 中間再沸器’而該供料物流部分也可提供熱負荷。其餘的 底部液體126 ’大體上稱為天然氣液,係供至NGL # 分館系統128。在那裏,NGL通常都降低壓力並且使用例 如去乙醇器、去丙醇器及/或去丁醇器等的習知分離裝置分 離以提供二或更多種烴部分。將該底部液體126分離成含 甲燒及乙烧附帶極少量丙烧的物流(該富含乙烧的物流)及 • 主要含匚3、C4及Cs+碳氫化合物(亦即正丙烷、異丙院及重 質物)的部分。典型地,該富含乙烷的物流13〇為去除乙醇 的塔頂部分並且含有少於約0.05%的丙烷。 該富含乙烷的第二種迴流物流136的使用使該分餾系 魯 統中能有高丙烷(96至99%)及丁烷(幾乎1〇〇%)回收率。 藉泵浦142以「吸收劑」液體140的形式抽取一部分 Cs +碳氫化合物,其係泵抽至洗滌塔壓力(亦即足以將其導 入該洗滌塔114的壓力,該壓力包括設備壓降及靜壓),在 ’ 熱父換器144中冷卻防備丙烧蒸發,進一步在主要熱交換 . 器122中冷卻’並且導入迴流筒11 8,與由NGL分餾所獲 得的第二種迴流物流或,如虛線所示,直接地混合。熱交 換器144可放置於該泵浦142之前或之後。 在導入該迴流筒11 8之前混合該吸收劑液體140與該 18 1314578 米'一^徑k、/;IL物流13 6传/土认由 你較佳的實施方式,因為能夠平衡並 且使部分吸收在該導管中進行。 如虛線所示,該哄立, Λ及收劑液體140可直接地供至該洗滌 塔114頂端或接近頂媳, 端 或在較佳的實施方式中,與該主 要熱交^器122上游的第—種塔頂蒸氣流116結合。 使富含乙烷的物流13〇在該熱交換器132中冷卻並且 局。ρ凝縮以防備丙烷蒸發,在主要熱交換器122中冷卻並 70王地凝縮,藉泵浦】34泵抽至該洗滌塔壓力,較佳地 與吸收劑液體140結合,並且以物流136的形式導入該迴 荀在該泵浦I34上游的任何未凝結的蒸氣可在該主要 熱交換器!22的中間管束中分離,凝縮,並且與該液化天 然氣產物124結合。 吸收劑液體140也可由例如c:3及C4碳氫化合物等的 NGL輕質產物獲得純的或摻混在—起。其可能主要地含有 C5碳氫化合物而沒有C6及可被額外的蒸餾塔排除在外的 更重成分。 物流130可為近乎純的乙烷,甲烷被額外的蒸餾塔排 除在外。一部分乙烷或乙烷_甲烷混合物可以產物的形式回 收。 使該第一種塔頂蒸氣流116在該主要熱交換器i 22
"J 暖管束中冷卻並且局部地凝縮,並且導至該迴流筒丨1 8。其 可在主要熱交換器122中冷卻之前先壓縮(未顯示)。該液 體部分以「第一種」迴流物流11 9的形式返回該洗務级 使該富含甲烧的「第二種」蒸氣部分120在該主要熱交換 19 1314578 器的中間及冷卻官束中液化並且較佳地低溫冷卻以提供 LNG 產物 1 24。 在較佳的實施方式中,使經局部地凝縮的第一種塔頂 蒸氣流116與該第二種迴流物流136及/或該吸收劑液體 140在該迴流筒118其中或上游結合使得部分平衡發生。藉 此,使該第一種液體迴流(經局部地凝.縮的第—種塔頂蒸氣 的液體部分)與該第二種液體迴流136及/或該吸收劑液體 14 0混合。 典型地’取決於天然氣供料組成物,該第二種迴流物 流13 6係低於該全部迴流(包括任何吸收劑液體)的約 20% ’而且該吸收劑液體14〇係低於該全部迴流的約1〇〇/〇。 若天然氧供料110不含適用於該吸收劑液體14〇的成分或 不含足量的成分’該等成分就可以額外供料的形式導入。 該第二種蒸氣流120可在導入主要熱交換器122之前 先壓,縮(未顯示)及/或在低溫冷卻之前先降低壓力。若將該 LNG產物124儲存在高壓(PNGL)下,就不需要在該冷卻束 管中低溫冷卻。 藉由蒸發再循環的冷凍劑(MR)流150並且分離成液體 152及輕質蒸氣156 (未顯示壓縮、冷卻及相分離)而冷卻該 主要熱交換器122,該冷凍劑流150係藉蒸發丙烷的多重 階段予以壓縮’冷卻。蒸氣156係凝縮,冷卻並且經節流 閥158而膨脹。液體丨52係冷卻,經由節流閥丨54膨脹, 並且與蒸發的凝縮蒸氣丨56結合。使結合的MR物流完全 地蒸發並且以物流1 50的形式離開該主要熱交換器1 22。 20 .1314578 節流閥154及/或156可利用等熵的緻密流體膨脹器,例如 液壓式涡輪,予以取代。任何其他的冷凍系統或系統的組 合,包括如US-A-630853 1中所說明的純流體瀑布及等熵蒸 氣膨脹’都可用於冷凍該主要熱交換器122。 第2圖顯示第1圖具體例的修飾例,其中該迴流筒u 8 以吸收塔21 8代替。將吸收劑液體丨4〇及/或該第二種迴流 物流136,較佳地二者皆結合於物流136中,供至該吸收 塔218的頂端。它們也可在相同位置或不同位置單獨地進 入該塔,而該二物流其中至少一者供至該吸收塔2 1 8的頂 端。舉例來說’吸收劑液體丨4 〇可供至該塔頂部以下或該 塔底部的某些階段。從該塔2丨8的頂部抽取該第二種塔頂 蒸氣流120 ’並且從該塔的底部抽取該第一種迴流物流 119。該塔218中的多重階段可從向上的蒸氣改善重質成分 的吸收。 第3圖顯示第1圖具體例的另一個修飾例’其中結合 該富含乙烧的物流130與吸收劑液體14〇而形成單流330。 使物流330在熱交換器332中冷卻並且局部凝縮以防備丙 燒蒸發,在主要熱交換器122中進一步冷卻並且完全地凝 縮,以泵浦334泵抽至該洗滌塔壓力,並且導入該迴流筒。 在較暖溫度下混合物流130及140並且使它們在一起凝縮 在熱力學上比第1及2圖所示的結構更有效率。當吸收在 熱交換器及332及122中進行時,益處與吸收塔218的益 處類似。此結構也免除該主要熱交換器丨22中的通道。如 第1圖的結構,物流116及33〇可在該主要熱交換器122 21 .1314578 的下游並在該迴流筒11 8之前結合。 第4圖顯示第3圖具體例的修飾例,其中將經結合之 富含乙烧的物流與吸收劑液體物流3 3 0供至相分離器4 3 0 中。該液體部分438藉泵浦432泵抽至該洗務塔114的壓 力,並且與該第一種塔頂蒸氣116在該主要熱交換器122 的上游結合。接著將流出該主要熱交換器丨22的結合物流 4 1 6供至該迴流筒11 8。小部分蒸氣4 3 6在該主要熱交換器 鲁 1 22中凝縮並且藉泵浦434泵抽並且導至該迴流筒11 8,視 需要地與物流4 1 6結合’或與液化天然氣在該主要熱交換 器12 2的低溫冷卻部分(冷卻束管)上游結合,其中該液體 ' 可在低溫冷卻之前先降低壓力。在該主要熱交換器122的 上游結合物流丨3〇與116及吸收劑液體140將進一步提高 該方法的熱力學效率。 視需要地,物流438可在導入該迴流筒118之前,先 在該主要熱交換器122的獨立迴路中冷卻。若物流1 30含 •有少許曱烧,甲烷可被洗滌塔i 14或該分餾系統的額外去 曱烷•塔排除在外’然後物流3 3 0可完全地凝縮並且不需要 相分離器430,沒有物流436,而且也可免除泵浦434。進 一步地’物流43 8可直接地供至該洗滌塔114,舉例來說供 . 至該塔頂端下方的第二個階段。 . 第5圖顯示第4圖具體例的修飾例,其中使經分離的 蒸氣部分436在壓縮器53〇中壓縮至該洗滌塔114的壓力, 在熱父換器5 3 2中冷卻並凝縮並且使所得的物流5 3 6與液 體部分438結合而形成物流538。熱交換器532可為一連 22 • 1314578 串的熱交換器,第一個使用冷卻水,其他的使用蒸發的丙 烷。物流438可在額外的熱交換器中壓縮之前先暖化至接 近室溫’並且接在該壓縮之後在後冷卻器及為了附加熱力 學效率的相同額外熱交換器中冷卻下來。物流536可為緻 密的超臨界流體。 第ό圖顯示第4圖具體例的另一個修飾例,其中藉著 在熱交換器612中,利用舉例來說,該迴流物流136及該 馨 吸收劑液體140之中任一或二者但較佳地藉由蒸發的丙 烧’冷卻而局部地凝縮該第一種塔頂蒸氣流丨丨。所得的第 —種二相物流在相分離器618中分離成「第二種」塔頂蒸 氣流61 6及富含曱烷的液流6丨9。該液流61 9以迴流的形 • 式返回洗滌塔11 4。使物流ό 16,處於匹配該主要熱交換p 122的底部溫度之溫度下,與物流438混合,在主要熱交 換器122中冷卻,並且以二相流626的形式供至該迴流筒 628。使來自該迴流筒628的塔頂蒸氣流62〇在該主要熱交 鲁 換器1 中液化並且以液化天然氣產物1 24的形式回收。 使來自該迴流筒628的液流629,視需要地在該主要熱交 換器122中再加熱,返回至該洗滌塔114與迴流液619相 同或不同的位置處。 • 相分離器618及/或迴流筒6284可利用底部具有二相 . (、料並由了頁部的冷卻流13 6及/或14 0提供迴流之吸收技予 以取代。 有關任何所舉例說明的具體例而說明的個別特徵,或 該等特徵的組合,都可適當地併入任何其他舉例說明的具 23 • 1314578 體例中。舉例來說,在有關第6圖所說明的主要熱交換器 122中視需要再加熱迴流物流629可應用於第1至5圖任 何的具體例。此外或替換地’藉衍生自第6圖具體例的第 種蒸氣塔頂部分116的液體部分619以供迴流至該洗滌 塔Π4也可應用於第丨至5圖任何的具體例。 實施例 使用第3圖的具體例’使97·9〇4磅莫耳/小時(44,4〇8 5 么斤莫耳/小時)之95〇磅/平方吋(65百萬帕)下的預純化天 然氣流11〇在熱交換器112中藉三階段的丙烷冷卻至-32 3 F (-35_7 C ) ’並且供至該洗滌塔U4。此供料物流丨1〇含有 0.6%氮氣、84.8%甲烷、7·3%乙烧、44%丙烷、〇7%異丁 烧、1.5%丁烧、〇.3%異戊烧' 〇 2%戊烧及〇 2%己烧類。該 塔114在8 4 0石旁/平方碎 十万寸(5·8百萬帕)下操作,並且具有藉由 丙烧冷卻的前兩個階段旁分出來桃物流m加熱的中間 再沸器及在約13(TF(5rc)下的底部再沸器128。塔頂部分 116在主要熱交換g 122的暖管束中從-以叫-” 4 卻至-77.5T (-60.8〇C ),祐曰丨v 人士& 7 並且以3有約15%液體的二相物 導入該迴流筒11 8。將洗滌技症加此、+ 爪 肝洗滌蝓底部物流126傳送至該分 統128,其由包含去乙醇写去 鮮器去丙醇器及去丁醇器的—查 串蒸餾塔組成。以去丙醇器的塔項部分的形式回 於該供料物流U。當"96%丙燒。以去丁醇器 = 分的形式回收到幾乎所有的丁烧及異丁院。使。^ 莫耳/小時⑽9公斤莫耳/小時)的流速及42平^ 24 .1314578 (2.9百萬帕)的壓力下含有約39%甲烧、61%乙烧及僅〇 〇5% 丙烧的去乙醇器塔頂部分與構成39%去丁烷器底部液體的 物流140混合;剩餘部分以C5 +產物的形式回收。低丙烷含 量對於高丙烷回收率而言很重要。物流14〇為處於17磅/ 平方吋(117千帕)及406磅莫耳/小時(184公斤莫耳/小時) 的流速下的液體,並且含有約51%異戊烷、36%戊烷、12% 己烷及少於1%的輕質成分。在與富含乙烷的物流13〇混合 之前先藉第3圖中未顯示的泵浦將物流14〇泵抽至至42〇 碎/平方对(2.9百萬帕)。使結合的物流3 3 0在熱交換器3 3 2 中藉丙烧冷卻至-32.3T (-35.7¾ )並且在主要熱交換器122 的暖管束中藉進一步地冷卻至_77 5下(_60 8。〇)而完全地凝 縮。將經凝縮的物流在泵浦334中泵抽至該洗滌塔壓力並 且導至該迴流筒118。使液體迴流119返回在-74.2T (-59.0 C )下的洗滌塔114頂部;在該相分離器中泵抽及混合會有 熱效應。物流120 ’其含有91.3%甲烷、7.8%乙烧、0.7% 氮氣' 0.2%丙烷及僅痕量的重質碳氳化合物,係處於_742 卞(_59.(TC )下並且具有83,571磅莫耳/小時(37,907公斤莫 耳/小時)的流速。使其在該主要熱交換器122的中間及冷卻 管束中冷卻至-161.6°F (-107.6°C ) ’然後以液體物流124的 形式降至15.3磅/平方吋(105.5千帕)的儲存壓力。如參照 第1圖所說明的’藉由包含氮氣、甲烷、乙烷及丙烷的混 合冷凍劑冷卻該主要熱交換器122。 咸將明白本發明並不限於以上參照較佳具體例而說明 的詳細内容,而且可進行許多修飾及變化而不會悖離如下 25 ♦1314578 列申請專利範圍所定義之發明範圍。 圖式簡單說明 在該等圖式中: 第1圖顯示本發明之一具體例; 第2圖,,肩示弟1圖具體例的修飾例其中該迴流筒(118) 以吸收塔(2 18)代替; • 第3圖顯不第1圖具體例的另一個修飾例,其中結合 s亥虽含乙烷的物流(130)與「吸收劑液體」物流而形成單流 (330); 第4圖顯示第3圖具體例的修飾例,其中經結合的第 • 二種迴流及吸收劑液體物流(3 3 0)係經相分離(43 0); 苐5圖顯示第4圖具體例的修飾例,其中壓縮,冷卻 並凝縮經分離的蒸氣部分(436),並且使所得的物流(536) 與該液體部分(438)結合;以及 籲 第6圖顯不苐4圖具體例的另一個修飾例,其中分兩 階段(6 12,122)凝縮來自該洗滌塔(114)的塔頂蒸氣(1 16)而 將分離的迴流物流(619,626)供至該洗滌塔。 26 * 1314578 主要元件符號說明 110 天然氣供料 112 熱交換器 114 洗滌塔 116 第一種塔頂蒸氣流 118 迴流筒 119 第一種迴流物流 120 第二種塔頂蒸氣流 122 熱交換器 124 液化天然氣產物 126 底部液體 127 底部液體 128 再沸器 130 富含乙烷的物流 132 熱交換器 134 泵浦 136 第二種迴流物流 140 吸收劑液體 142 果浦 144 熱交換器 150 物流 150 冷凍劑流 150 加工流 152 液體 154 節流閥 156 輕質蒸氣 158 節流閥 218 該吸收塔 330 單流 332 熱交換器 334 泵浦 416 物流 430 相分離Is 432 泵浦 434 泵浦 436 蒸氣 438 液體部分 530 壓縮器 532 熱交換器 536 物流 538 物流 612 熱交換器 616 第二種塔頂蒸氣流 620 塔頂蒸氣流 628 迴流筒 27
Claims (1)
1314578 十、申請專利範圍: 1. 一種從曱烷在含乙烷及更重的碳氫化合物之混合物中之 供料回收比甲烧更重的成分之方法,該方法包含: 將該供料導入洗滌塔的第一個位置; 從該洗滌塔抽出比甲烷更重的成分中摒除的第一種拔頂 蒸氣流及富含比甲烧更重的成分之底部物流; 冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成第—種 二相物流; 分離該第一種二相物流以提供第二種塔頂蒸氣流及富含 曱烧的第一種迴流物流; 將該富含甲烷的第一種迴流物流導入該洗滌塔第—個位 置上方的第二個位置;以及 將該底部物流分離成富含乙院的物流及一或多種富含比 乙院更重的成分之物流; 改良之處在於富含乙烷的第二種迴流物流係衍生自該富 含乙烧的物流,並且在選自該洗滌塔第一個位置上方的第 二個位置及第三個位置之位置導入該洗滌塔。 2. 如申請專利範圍第1項之方法,其中在低於導入該洗滌 塔的供料溫度之溫度下凝縮該富含乙烷的物流,並且在 以富含乙烷的第二種迴流物流的形式導入該洗滌塔之前 先泵抽經凝縮的物流。 3. 如申請專利範圍第2項之方法,其中該溫度係低於-32°F。 4. 如申請專利範圍第1項之方法,其中該供料為冷卻的天 然氣供料。 28 .1314578 項之方法,其中該富含乙烧的第二 甲烷的第一種迴流物流分開地供入 5.如申請專利範圍第! 種迴流物流與該富含 該洗蘇塔。 .如申請專利範圍第i項之方法,其中該富含乙烷的第 種AL物办L在^入該洗條塔之前先與該富含甲烧的第 種迴流物流混合。 第二 迴流
7.如申請專利範圍“項之方法,其中該富含乙烷的 種迴流物流與該富含甲烷的第一種迴流物流在選自 筒的上游及其中之位置處結合。 8. 如申請專利_ 6項之方法,其中該第一種二相物流 係供至該富令Λ检ΑΑ Λ* 含乙烷的第二種迴流物流以迴流的形式供入 的吸收塔底部。 9. 如申清:利範圍帛6項之方法,其中該富含乙烷的物流 在與該田3甲烷的第_種迴流物流混合之前先完全地凝 縮。 10 ·如申請專利節图筮,τ 軌圍第1項之方法,其中該富含乙烷的物流 係去乙烷器的蒸氣塔頂部分。 如申明專利範圍第1項之方法,其中衍生自富含比乙烷 更重的成为之一或多種物流的吸收劑液體在選自該洗滌 塔第個位置上方的第二個位置、第三個位置及第四個 位置之位置導入該洗滌塔。 12·如申明專利範圍第11項之方法,其中該吸收劑液體(140) 包含戊烷及異戊烷。 13.如申明專利範圍第u項之方法,其中該吸收劑液體包 29 ι 1314578 含C4 ^^風化合物。 14.如申明專利範圍第丨丨項之方法其中該吸收劑液體包 含C5 +碳氫化合物。 15·如申請專利範圍帛11項之方法,其中該吸收劑液體與 該虽含乙烷的第二種迴流物流或該富含曱烷的第一種迴 流物流分開地供入該洗滌塔。 16·如申μ專利範圍帛丨丨項之方法,其中該吸收劑液體在 與導入该洗滌塔之前先與該富含甲烷的第一種迴流物流 及邊虽含乙烷的第二種迴流物流其中至少一者結合。 17.如申1專利圍帛i 6項之方法’其中該吸收劑液體與 該富含曱烷的第—種迴流物流及該富含乙烷的第二種迴 /;IL物机中至少一者在選自迴流筒的上游及其中之位置 處結合。 18-如申請專利範圍第16項之方法,其中該第—種二相物 流係供至該吸收劑液體及該富含乙烷的第二種迴流物流 其中至y者以迴流的形式供入的吸收塔底部。 11如申叫專利圍第j 6項之方法,其中該吸收劑液體在 該第種塔頂蒸氣流局部凝縮之前先與該第一種塔頂蒸 氣流結合而形成第一種二相物流。 2〇—如申,專利範圍帛11項之方法,其中該吸收劑液體在 富含氣態乙烷的物流局部凝縮之前先與該富含氣態乙烷 的物流結合以提供第二種迴流物流。 21.如申請專利範圍帛2〇項之方法,其中使結合的吸收劑 液體與富含氣態乙烷的物流相分離,並且將液體部分供 1314578 至該洗滌塔第一個位置上方。 22.如申請專利範圍帛21項之方法,其中使蒸氣部分凝縮 並且供至該洗滌塔第一個位置上方。 如申明專利圍第21項之方法,其中該液體部分在該 第種塔了頁物流局部凝縮之前先與該第一種塔頂物流結 合以提供第一種二相物流。
'如申請專利_ 21項之方法,其中經凝縮的蒸氣部 刀在該第一種塔頂物流局部凝縮之前先與該第—種塔頂 物流結合以提供第一種二相物流。 ° 25.如申請專利_ 24項之方法,其中該經凝縮的落氣 部分與液體部分在該第一種塔頂物流局部凝縮之前先斑 該第-種塔頂物流結合以提供第一種二相物流。 从如申請專利_ β之方法,其中該第一種塔頂物流 分兩階段局部地凝编,并 、、 並具將來自各個凝縮的液體部分 以迴流的形式供至該洗滌塔。 27. 如申請專利_ 1項之方法,其中該富含甲烧的第一 種:α抓物抓構成全部迴流(亦即供至該洗滌塔第一個位 置上方的液體)的至少約8〇%。 28. 如申請專利範圍第彳@ 項之方法,其中該第二種迴流物流 係少於全部迴流(亦即供至該洗條塔第一個位置上方的 液體)的約20%。 項之方法,其中該吸收劑液體係 至該洗務塔第一個位置上方的液 29·如申請專利範圍第u 少於全部迴流(亦即供 體)的約10%。 31 • 1314578 30.如申請專利範圍第1項之方法,其中該第二種迴流物流 含有少於約〇.〇5°/。的丙烷。 31_如申請專利範圍第1項之方法,其中從富含乙烷的物流 移除甲烷,藉以該第二種迴流物流基本上由乙烷組成。 32_如申清專利範圍第i項之方法’其中多於9〇%的丙烷係 以產物的形式從該底部物流回收得到。 33·如申請專利範圍第丄項之方法,其中多於9〇〇/〇的丁烷係 以產物的形式從該底部物流回收得到。 34. 如申請專利範圍第【項之方法,其中使第二種塔頂蒸氣 液化以提供液化天然氣(LNG)產物。 35. —種藉由申請專利範圍第丨項的方法從曱烷在含乙烷及 更重的碳氫化合物之混合物中之供料回收比甲烷更重的 成分之裝置,該裝置包含: 一洗滌塔; 用於將該供料導入洗滌塔第一個位置的的導管裝置; 用於從該洗滌塔抽出比甲烷更重的成分中摒除的第一種 塔頂蒸氣流及富含比曱烷更重的成分之底部物流的導管裝 置; 用於冷卻並且局部地凝縮該第一種塔頂蒸氣流而形成第 一種二相物流的熱交換裝置; 用於分離該第一種二相物流以提供第二種塔頂蒸氣流及 富含甲烷的第一種迴流物流的分離裝置; 用於將該富含甲烧的第一種迴流物流導入該洗滌塔第一 個位置上方的第二個位置的導管裝置; 32 ‘1314578 用於將該底部物流分離成富含乙炫的物流及一或多種富 3比乙烷更重的成分之物流的分離裝置;以及 用於選自第-個位置上方的第二個位置及第三個位置之 位置處,將衍生自該富含乙燒的物流之富含乙烧的第二種 迴流物流導入該洗滌塔的導管裝置。
36. 如申請專利範圍f 35項之裝置,其包含用於低於導入 該洗滌塔的供料溫度之溫度下凝縮該富含乙烷的物流的 熱交換裝置,以及用於以富含乙烷的第二種迴流物流的 形式導入該洗滌塔之前泵抽經凝縮的物流的泵抽裝置。 37. 如申請專利範圍第35項之裝置,其包含一迴流筒,該 富含乙烷的第二種迴流物流與該富含曱烷的第一種迴流 物流由該迴流筒供入該洗務塔。 38·如申請專利範圍第35項之方法,其包含一吸收塔,該 吸收塔接收呈底部供料形式的第一種二相物流及呈迴流 形式的富含乙烷的第二種迴流物流,並且該底部液體從 該吸收塔供至該洗滌塔。 39·如申請專利範圍第35項之裝置,其包含用於選自該第 一個位置上方的第二個位置、第三個位置及第四個位置 之位置處’將富含比乙烷更重的成分且由用於分離該洗 滌塔的底部物流所提供之吸收劑液體導入該洗滌塔的導 管裝置。 40.如申請專利範圍第39項之裝置,其包含一迴流筒’該 吸收劑液體與該富含曱烷的第一種迴流物流及該富含乙 烷的第二種迴流物流其中至少一者的混合物從該迴流筒 33 1314578 供至該洗滌塔。 札如申請專利卿39項之方法,其包含一吸收塔,該 吸收塔接收呈底部供料形式的第—種二相物流及呈迴流 形式的吸收劑液體與富含乙烷的第二種迴流物流其中至 少一者,並且該底部液體從該吸收塔供至該洗滌塔。 42. 如申請專利範圍第39項之裝置,其包含用於使該吸收 劑液體在該第一種塔頂蒸氣流局部凝縮之前先與該第一 # 種塔頂蒸氣流結合而形成第一種二相物流的裝置。 43. 如申請專利範圍帛39項之裝置,其包含用較該吸收 劑液體在該富含氣態乙烷的物流凝縮之前先與該富含氣 態乙烷的物流結合而形成第二種二相物流的裝置。 * 认如申請專利範圍帛則之裝置,*包含用於使結合的 吸收劑液體與富含氣態乙烷的物流相分離的分離裝置, 以及用於將液體部分供至該洗滌塔第一個位置上方的導 管裝置。 _ 45_如巾請專利範圍第44項之裝置,其包含用於使蒸氣部 分凝縮的熱交換裝置以及用於供至該洗滌塔第一個位置 上方的導管裝置。 46·如申請專利議44項之裝置’其包含用於使該液體 . 部分在該第一種塔頂物流局部凝縮之前先與該第一種塔 . 頂物流結合以提供第一種二相物流的裝置。 47.如申請專利範圍帛44項之裝置,其包含㈣使經凝縮 的蒸氣部分在該第一種塔頂物流局部凝縮之前先與該第 一種塔頂物流結合以提供第一種二相物流的裝置。 34 ‘1314578 48.如申請專利範圍第ο項 項裝置,其包含用於使該經凝 縮的蒸氣部分與液體邱八力绿银 體口P刀在該第一種塔頂物流局部凝縮 之刖先與該第一種级τ首板故丛Λ °頂物"L結合以提供第一種二相物流 的裝置。
49_如申請專利範圍 局部地凝縮該第 第35項之襄置,其包含用於分兩階段 一種塔頂物流並且將來自各個凝縮的液 體部分以迴流的形式供至該洗滌塔的裝置。 35
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- 2006-05-15 RU RU2007147253/06A patent/RU2367860C1/ru not_active IP Right Cessation
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SG148188A1 (en) | 2008-12-31 |
US20100024477A1 (en) | 2010-02-04 |
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MX2007014475A (es) | 2008-02-11 |
RU2367860C1 (ru) | 2009-09-20 |
MY142025A (en) | 2010-08-16 |
JP2008545819A (ja) | 2008-12-18 |
EP1883773A1 (en) | 2008-02-06 |
RU2007147253A (ru) | 2009-06-27 |
KR20080015819A (ko) | 2008-02-20 |
AU2006248647A1 (en) | 2006-11-23 |
KR100939053B1 (ko) | 2010-01-28 |
TW200641114A (en) | 2006-12-01 |
WO2006123240A1 (en) | 2006-11-23 |
US20060260355A1 (en) | 2006-11-23 |
CN101268325A (zh) | 2008-09-17 |
AU2006248647B2 (en) | 2009-09-03 |
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