WO2023030679A1 - Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage - Google Patents
Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage Download PDFInfo
- Publication number
- WO2023030679A1 WO2023030679A1 PCT/EP2022/025388 EP2022025388W WO2023030679A1 WO 2023030679 A1 WO2023030679 A1 WO 2023030679A1 EP 2022025388 W EP2022025388 W EP 2022025388W WO 2023030679 A1 WO2023030679 A1 WO 2023030679A1
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- WO
- WIPO (PCT)
- Prior art keywords
- column
- pressure
- rectification
- argon
- low
- Prior art date
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- 238000000926 separation method Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 32
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims abstract description 348
- 229910052786 argon Inorganic materials 0.000 claims abstract description 174
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 76
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000007789 gas Substances 0.000 claims abstract description 48
- 239000012530 fluid Substances 0.000 claims abstract description 41
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 38
- 238000012546 transfer Methods 0.000 claims description 36
- 239000007788 liquid Substances 0.000 claims description 30
- 230000008569 process Effects 0.000 claims description 20
- 238000010992 reflux Methods 0.000 claims description 5
- 239000000047 product Substances 0.000 description 31
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 25
- 239000001301 oxygen Substances 0.000 description 25
- 229910052760 oxygen Inorganic materials 0.000 description 25
- 238000001704 evaporation Methods 0.000 description 20
- 230000008020 evaporation Effects 0.000 description 17
- 238000013461 design Methods 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 10
- 230000006835 compression Effects 0.000 description 8
- 238000007906 compression Methods 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 230000009467 reduction Effects 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000605 extraction Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000006870 function Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000012356 Product development Methods 0.000 description 1
- 210000001015 abdomen Anatomy 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000004781 supercooling 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
- 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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of 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
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04096—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of argon or argon enriched 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
- 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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/0423—Subcooling of liquid process 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
- 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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)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
- 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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
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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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
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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
- F25J3/04—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 for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
- F25J3/04715—The auxiliary column system simultaneously produces oxygen
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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
- F25J3/04—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 for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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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
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
- F25J3/048—Argon 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
- 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
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
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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
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
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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
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/08—Processes or apparatus using separation by rectification in a triple pressure main column system
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/52—Oxygen production with multiple purity O2
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
-
- 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
- F25J2270/02—Internal refrigeration with liquid vaporising loop
Definitions
- the present invention relates to a method for the low-temperature separation of air and an air separation plant according to the respective preambles of the independent patent claims.
- Air separation plants have rectification column arrangements that can be designed in different ways.
- rectification columns for obtaining nitrogen and/or oxygen in the liquid and/or gaseous state i.e. rectification columns for nitrogen-oxygen separation, which can be combined in particular in a known double column, rectification columns for obtaining other air components, in particular noble gases, or from be provided pure oxygen.
- the rectification columns of typical rectification column arrangements are operated at different pressure levels.
- Known double columns have a so-called pressure column (also referred to as a high-pressure column, medium-pressure column or lower column) and a so-called low-pressure column (upper column).
- the high-pressure column is typically operated at a pressure level of 4 to 7 bar, in particular about 5.3 bar, while the low-pressure column is operated at a pressure level of typically 1 to 2 bar, in particular about 1.4 bar.
- higher pressure levels can also be used in these rectification columns.
- the pressures given here and below are absolute pressures at the top of the rectification columns given in each case.
- Air separation plants can be designed differently depending on the air products to be delivered and their required aggregate and pressure conditions.
- So-called internal compression is known, for example, for the provision of gaseous pressure products.
- a cryogenic liquid is removed from the rectification column arrangement, subjected to an increase in pressure in the liquid state and converted into the gaseous or supercritical state by heating.
- internally compressed gaseous oxygen, internally compressed gaseous nitrogen or internally compressed gaseous argon can be produced in this way.
- Internal compression offers a number of advantages over external compression, which is also possible as an alternative, and is explained, for example, in Häring (see above), Section 2.2.5.2, "Internal Compression".
- the present invention sets itself the task of specifying means which further improve the provision of air products, in particular in accordance with the requirement profile explained, and make them more efficient and simpler.
- the invention is intended to provide a solution by means of which (ultra)high-purity oxygen in a liquid or gaseous state can be obtained in addition to the air products mentioned. Disclosure of Invention
- the present invention proposes a method for the low-temperature separation of air and an air separation plant with the features of the respective independent patent claims. Configurations are the subject matter of the dependent patent claims and the following description.
- a “condenser evaporator” refers to a heat exchanger in which a first, condensing fluid stream enters into indirect heat exchange with a second, evaporating fluid stream.
- Each condenser evaporator has a condensing space and an evaporating space.
- Condensation and evaporation chambers have liquefaction and evaporation passages. The condensation (liquefaction) of the first fluid stream is carried out in the liquefaction chamber, and the evaporation of the second fluid stream is carried out in the evaporation chamber.
- the evaporating and condensing spaces are formed by groups of passages which are in heat exchange relationship with each other.
- Condenser evaporators are also referred to as “top condenser” and “bottom evaporators” according to their function, with a top condenser being a condenser evaporator in which the top gas of a rectification column is condensed and a bottom evaporator being a condenser evaporator in which the bottom liquid of a rectification column is evaporated.
- top condenser being a condenser evaporator in which the top gas of a rectification column is condensed
- a bottom evaporator being a condenser evaporator in which the bottom liquid of a rectification column is evaporated.
- bottom liquid can also be evaporated in a top condenser, for example as used in the context of the present invention.
- expansion turbine or “expansion machine” which can be coupled to other expansion turbines or energy converters such as oil brakes, generators or compressors via a common shaft, is set up to expand a gaseous or at least partially liquid material flow.
- expansion turbines for use in the invention can be designed as turboexpanders.
- a so-called residual gas turbine can be used in particular, which expands impure nitrogen from the rectification column arrangement to obtain cold.
- Fluids i.e. liquids and gases, as used herein, may be rich or poor in one or more components, with “rich” meaning at least 50%, 75%, 90%, 95%, 99%, 99.5% , 99.9% or 99.99% and “poor” for a content not exceeding 50%, 25%, 10%, 5%, 1%, 0.1% or 0.01% by mole, weight or volume base can stand.
- the term “predominantly” may correspond to the definition of "rich”.
- Fluids may also be enriched or depleted in one or more components, which terms refer to a content in a source fluid from which the fluid was derived.
- the fluid is "enriched” when it has at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times, 100 times or 1,000 times the content, and “depleted” when this contains at most 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of a corresponding component, based on the starting fluid. If, for example, “oxygen” or “nitrogen” is mentioned here, this also includes a fluid that is rich in oxygen or nitrogen, but does not necessarily have to consist exclusively of them.
- high purity oxygen (or “oxygen 6.0”) is to be understood here as meaning liquid oxygen (HLOX) or gaseous oxygen (HGOX) with an oxygen content of at least 99.9999 mole percent. In other words, there is a maximum of 1 ppm total impurities (mainly argon and methane) here.
- ultra-high purity oxygen is intended accordingly to denote oxygen with an even higher oxygen content, in particular at least 99.99999 mole percent. When speaking of the formation of high purity oxygen, this can also include the formation of ultra high purity oxygen.
- pressure range and "temperature range” to characterize pressures and temperatures, which is intended to express the fact that corresponding pressures and temperatures in a corresponding system do not have to be used in the form of exact pressure or temperature values in order to to realize the inventive concept.
- pressure range and temperature ranges
- Corresponding pressure ranges and temperature ranges may be disjoint ranges or ranges that overlap one another.
- Absolute and/or relative spatial information used below refer here in particular to the spatial orientation of the correspondingly designated elements of an air separation plant, for example Rectification columns, sub-columns of multi-part rectification columns, or rectification areas of rectification columns in normal operation.
- An arrangement of two elements "on top of each other” is understood here in particular to mean that the upper end of the lower of the two elements is at a lower or the same geodetic height as the lower end of the upper of the two elements and the projections of the two elements on a horizontal plane intersect .
- the two elements can be arranged exactly one above the other, i.e.
- rectification area is intended here to refer to any section within a rectification column or column section of a multi-part rectification column that is set up for carrying out a rectification and is designed for this purpose in particular with appropriate mass transfer structures such as separating trays or ordered or disordered packing. In particular, can be provided between rectification areas fluid withdrawals or feed points, for example side withdrawals.
- the "bottom” of the rectification column is located below a (functionally) lowest rectification area, and its “top” is above the (functionally) upper rectification area.
- a “nitrogen section” is the uppermost region of a low-pressure column that may be provided, which is provided in order to be able to draw off (substantially) pure nitrogen at the top thereof.
- argon although present in atmospheric air at a level of less than 1 mole percent, exerts a strong influence on the concentration profile in the low pressure column.
- the separation in the lowermost separation section of the low pressure column which typically comprises 30 to 40 theoretical or practical plates, can be regarded as an essentially binary separation between oxygen and argon.
- This rectification area is also referred to as the "oxygen section”. Only from the exit point for the gas transferred to the crude argon column does the separation change to a ternary separation of nitrogen, oxygen and argon within a few theoretical or practical trays.
- a double column arrangement with a pressure column and a low-pressure column can be operated at an increased pressure level in a particularly advantageous manner, with nitrogen is drawn off at the top of the low-pressure column and part of it is heated, compressed, cooled again in the form of a recycle stream and into which the double column arrangement, i.e. the pressure column and/or the low-pressure column, is fed.
- the recycle stream can optionally (proportionally or partially or completely) be passed through the main condenser and/or through a bottom evaporator of the pure oxygen column before it is fed into the pressure column and/or the low-pressure column.
- the top gas of the pressure column comprises further purified recycle stream fluid.
- a portion of the top gas of the pressure column can be passed through the main condenser and/or through the bottom evaporator of the pure oxygen column and a further portion can be recovered as nitrogen product.
- a certain proportion of the circulating stream which in this case is at least partly fed into the pressure column can therefore be taken off again from the pressure column, in other words, above the point at which it is fed into the pressure column.
- the nitrogen-rich fluid contained in the circulating stream can be further purified and made available as a product.
- the low-pressure column in particular is set up by using a suitable nitrogen section in the upper region to provide a corresponding nitrogen-rich top gas with the specifications explained below, which is used in the formation of the recycle stream.
- one or more additional rectification columns for argon production for example a crude argon column and a pure argon column of a known type, are also used.
- a crude argon column and a pure argon column it is also possible to provide a single column for obtaining an argon product, which partially combines the functions of crude and pure argon columns by having a further section provided for separating nitrogen.
- an argon column is mentioned below, this can in particular be a crude argon column that is present in addition to a pure argon column, but also a correspondingly modified crude argon column that does not have a pure argon column in addition to it.
- a pure oxygen column can also be used in such a process, which is set up to obtain high-purity or ultra-high-purity oxygen in the sense explained and which is fed from an intermediate point of the argon column with liquid which is fed in at the top of the pure oxygen column.
- the argon column can also be designed in two parts, with a functionally lower part of the argon column up to the mentioned intermediate point in a common Column jacket can be accommodated with the pure oxygen column, and the functionally upper part is arranged separately therefrom.
- FIG. 2 shows, for example, a separate pure oxygen column that is not combined with parts of the argon column.
- the rectification process in the pure oxygen column is driven by the evaporation of the bottom liquid using a bottom evaporator (reboiler).
- the circuit stream mentioned can be used as the heating medium for this bottom evaporator, which can be conducted in particular at least partially in parallel through the main condenser, which connects the pressure column and the low-pressure column in a heat-exchanging manner, and the bottom evaporator.
- its top gas can also be used in a corresponding manner.
- Such a topology may have certain advantages compared to an implementation using pressurized air that is appropriately condensed.
- the main condenser which connects the pressure column and the low-pressure column in a heat-exchanging manner, is designed with a comparatively low average temperature difference (approx. 1.0 K or slightly above), which also results in the low average temperature difference in the bottom evaporator of the pure oxygen column (approx 1.0 K or slightly below, taking into account a certain pressure drop for the control valve in the partial flow of the circulating flow or of the top gas of the pressure column to this bottom evaporator).
- the main condenser would have to be designed with a significantly larger average temperature difference in order to have enough leeway (differential pressure) for the control valve in the circulating flow or its partial flow or top gas of the pressure column upstream of the bottom evaporator of the pure oxygen column in all operating cases to have.
- leeway Differential pressure
- An essential aspect of the invention consists in particular in separating the pressure chambers of the double column and argon column by providing an additional valve and, in configurations, by providing a sufficient difference in height for returning liquid from the argon column to the low-pressure column. This is not required when in other configurations the low pressure column is split above the oxygen section with liquid recycle via a pump
- the additional valve can be fully (or almost fully) opened in the design case and partially closed in all cases with a greatly reduced load ratio between the two mentioned condensers, which leads to a reduced operating pressure in the argon column and the pure oxygen column.
- the reduced volume flow into the argon column is irrelevant, since it is operated with a reduced mass flow compared to the design case.
- the cases with a reduced load ratio between the main condenser and the bottom evaporator of the pure oxygen column are underload cases, ie operating cases with a lower process air flow.
- the proposed solution enables robust plant operation in cases with a greatly reduced main product (gaseous compressed nitrogen) and relatively high extraction of the pure oxygen product and/or lower oxygen content in the feed stream into the pure oxygen column without leading to an efficiency disadvantage in the design case.
- the introduction of the valve mentioned alone leads to a sufficient differential pressure for the control valve in the heating medium flow upstream of the bottom evaporator of the pure oxygen column.
- the present invention proposes a method for the low-temperature separation of air using an air separation plant which has a rectification column arrangement with a pressure column, a low-pressure column and an argon column, the low-pressure column being constructed in one or more parts and having a first and a second rectification region (in the case of a one-piece Formation in a common column shell, otherwise distributed over several column shells) and the argon column is formed in one or more parts and has a first and a second rectification area (in the case of a one-piece formation in a common column shell, otherwise distributed over several column shells).
- the first rectification area of the low-pressure column and the argon column is in particular the (functionally) lowest one, and the second rectification area is directly above it.
- the pressure column and the low-pressure column are operated in particular in such a way that a bottom liquid of the pressure column, which is fed with at least feed air, has a content of 28 to 38% oxygen as well as argon and nitrogen and a top gas of the pressure column has a content of 0.001 to 100 ppb , for example approx. 10 ppb oxygen, 0.1 to 100 ppm, for example approx. 30 ppm argon, and otherwise essentially nitrogen and possibly lighter components.
- the pressure column and the low-pressure column are also operated in particular in such a way that the top gas of the low-pressure column has a content of 0.001 to 1000 ppb, for example approx. 10 ppb, oxygen and 0.1 to 300 ppm, for example approx. 35 ppm argon.
- An argon-enriched first transfer fluid is removed from the low-pressure column between the first and the second rectification region of the low-pressure column, in particular at the known argon belly, and fed into the argon column in a first transfer quantity below the first rectification region of the argon column.
- the operation of the argon column corresponds to known methods in which a corresponding argon column is fed with a corresponding fluid.
- an argon-depleted second transfer fluid is removed from the argon column and fed (recycled) into the low-pressure column in a second transfer rate between the first and second rectification sections of the low-pressure column, as is also known to this extent in the field of argon recovery.
- the first transfer fluid is enriched in argon, in particular compared to a bottom liquid of the low-pressure column and compared to its top gas.
- argon in particular, it can contain 20 to 6%, for example 18 to 11%, argon and the remainder predominantly oxygen.
- the removal takes place at a point between corresponding rectification areas, which are known to the person skilled in the art.
- the air separation plant is operated in a first operating mode and in a second operating mode, with a nitrogen product being discharged from the air separation plant in a larger product quantity in the first operating mode than in the second operating mode.
- the nitrogen product can be formed in the manner previously indicated and discussed below.
- the first operating mode represents in particular the explained design case
- the second operating mode corresponds to a special operating mode or the non-design case with reduced nitrogen extraction.
- the pressure in the argon column is reduced, while in the Low-pressure column made a lower or no pressure reduction and the pressure is kept there in particular substantially constant.
- the pressure reduction takes place in particular in the manner explained below.
- the conversion in the argon column is typically adjusted by means of a gas valve at the outlet of the evaporation space of the top condenser of the argon column, a condenser evaporator. If, for example, a lower conversion quantity is required (e.g. for the case of underload), the flap is closed more tightly and the pressure in the evaporation chamber is increased as a result. The increase in pressure leads to an increase in the evaporation temperature and (thereby) to a reduction in the driving temperature difference in the condenser evaporator. With a smaller temperature difference, less argon can be condensed in the condenser evaporator and the conversion decreases.
- a gas valve at the outlet of the evaporation space of the top condenser of the argon column, a condenser evaporator.
- the pressure in the argon column is still the same as in the low-pressure column. If a valve in the feed into the argon column from the low-pressure column is now closed, the pressure in the argon column is reduced.
- the pressure reduction also leads to a reduction in the condensation temperature (and thereby also the driving temperature difference in the condenser evaporator). This would lead to a further reduction in sales.
- a suitable regulation therefore "maintains" the conversion by adjusting the aforementioned gas flap at the outlet of the evaporation chamber, i.e. the flap is opened more in this case, so that the evaporation pressure is reduced and the conversion quantity remains unchanged.
- the argon column is operated under reduced pressure and with the same conversion (suitable for the case of underload).
- the argon column can also be operated under slightly reduced pressure even in the first operating mode; then its operating pressure is further reduced in the second operating mode.
- adjusting the pressure in the argon column in a first step includes in particular increasing the pressure in an evaporation chamber of a top condenser of the argon column, increasing the evaporation temperature in the evaporation chamber and reducing a driving temperature difference and the conversion in the argon column.
- the adjustment of the pressure in the argon column includes in particular a closing or stronger closing of the aforementioned valve in the feed line.
- the argon column includes in particular a pressure reduction in the evaporation space of the top condenser of the argon column, reducing the evaporation temperature in the evaporation space and increasing a driving temperature difference and the conversion in the argon column.
- a pressure is set in the argon column in a pressure range which, in the first operating mode, corresponds to a pressure range in which the low-pressure column is operated and which, in the second operating mode, is below the pressure range in which the low-pressure column is operated.
- the valve mentioned which is provided in a line provided for feeding the first transfer quantity into the low-pressure column, can only be closed in the second operating mode or in the second operating mode more than in the first operating mode.
- This valve takes care of the pressure loss or the lower operating pressure in the argon and, if necessary, the pure oxygen column, while a conversion quantity in the argon column, as is known and just explained, is controlled via a valve at the outlet from an evaporation chamber of the crude argon condenser (i.e. of the top condenser of the argon column) can be adjusted.
- the amount of conversion in the argon column is significantly smaller in the second operating mode because the amount of feed air is significantly smaller.
- the rectification column arrangement has a pure oxygen column in which a pressure is set in a pressure range which, in the first operating mode, corresponds to the pressure range in which the low-pressure column is operated, and which in the second operating mode is below the pressure range , in which the low-pressure column is operated.
- the pure oxygen column is operated with a liquid as reflux, which is withdrawn from the argon column between the first and second rectification regions of the argon column, and a top gas is withdrawn from the pure oxygen column and is fed into the argon column between the first and second rectification regions of the argon column.
- the invention can be adapted to load changes between the main condenser and the bottom evaporator of the pure oxygen column offer particular advantages.
- the present invention can be advantageous when a circulatory flow is formed, as already described in principle above.
- the pressure column and the low-pressure column are, as is generally customary, connected in a heat-exchanging manner by means of a main condenser, with the use of overhead gas from the low-pressure column forming a circulatory stream which is heated, compressed, cooled again, partly or completely through the main condenser and/or to partially or completely through a bottom evaporator of the pure oxygen column, at least partially condensed there, and fed back into the rectification column arrangement, i.e. the pressure column and/or the low-pressure column.
- the compression takes place in particular on the warm side of the main heat exchanger.
- this overhead gas may be carried up to this point along with the remainder used to form the recycle stream, and the nitrogen product in this case may be upstream or downstream the compression is branched off from the circulating flow.
- Part or all of the circulating stream can be passed through the main condenser and/or part or all of it through a bottom evaporator of the pure oxygen column, at least partially condensed there, and returned to the rectification column arrangement.
- the circulating stream is fed, in particular completely, into the pressure column without first passing it through the main condenser and/or the bottom evaporator of the pure oxygen column.
- gas in particular top gas
- the nitrogen product can be provided using top gas from the pressure column, with the pressure column being fed at least a proportion of the circuit stream for this purpose in the embodiment mentioned with additional purification of the circuit stream.
- the nitrogen-rich fluid of the circulating stream is thus further purified in the pressure column in order to obtain a correspondingly pure product.
- the nitrogen product can also be provided using top gas of the low-pressure column that is not fed into the pressure column in the form of the recycle stream.
- the nitrogen product is branched off in particular on the hot side of the main heat exchanger and in particular before or after a corresponding compression of a remainder of the top gas used to form the circulating stream.
- a product quantity of the nitrogen product that is discharged from the air separation plant in the second operating mode can be at least 2.5% lower, at least 10% lower or 10% to 60% lower than in the first operating mode.
- a pressure that is at least 50 mbar, at least 100 mbar and/or up to 700 mbar or up to 900 mbar lower than in the low-pressure column can be set in the argon column, while a pressure in the low-pressure column is kept essentially constant, i.e. does not change by more than 100 mbar.
- the first rectification area and the second rectification area of the low-pressure column can be accommodated in a common column shell, in which the second rectification area of the low-pressure column is arranged above the first rectification area of the low-pressure column.
- This first group of embodiments of the invention thus relates to an "undivided" low-pressure column. Variants of this first group of configurations of the invention are initially described below.
- Rectification area of the argon column especially in separate column jackets be accommodated, wherein the column jacket, in which the first rectification region of the argon column is accommodated, is arranged above a column jacket of the pure oxygen column and is connected to it or formed in one piece with it.
- the first rectification region of the argon column and the pure oxygen column can therefore be arranged in a common external structure, fluidically separated.
- the first rectification region of the low-pressure column can be accommodated in a first column jacket
- the second rectification region of the low-pressure column can be accommodated in a second column jacket
- the first and second column jackets can be arranged next to one another.
- the first column jacket and a column jacket, which surrounds the pressure column are arranged in particular one above the other and are designed in the form of a double column.
- the functionally lower part of the low-pressure column is therefore placed on top of the pressure column.
- the second rectification area of the argon column can be divided into a first partial area and a second partial area, with the first rectification area of the argon column being accommodated in a third column jacket, the first partial area of the second rectification area of the argon column being above the first rectification area of the argon column is housed in the third column shell, and the second portion of the second rectification section of the argon column is housed in the fourth column shell.
- gas can be withdrawn from the first column shell above the first rectification region of the low-pressure column and, in a first portion below the second rectification region of the low-pressure column, into the second column shell and in a second portion below the first rectification region of the argon column as the first transfer fluid be fed into the third column shell.
- liquid below the first rectification region of the argon column from the third column jacket and fed into the first column jacket above the first rectification section of the low pressure column as the second transfer fluid and liquid may be withdrawn from the second column jacket below the second rectification section of the low pressure column and fed into the third column jacket below the first rectification section of the argon column.
- a lower termination of the second column jacket is arranged in particular geodetically above a feed position of the first transfer fluid into the third column jacket, so that the first transfer fluid can be transferred into the third column jacket purely by gravity, i.e. in particular without using a pump.
- the first pressure level is 9 to 14.5 bar, for example about 11.8 bar, at the top of the first rectification column and the second pressure level is 2 to 5 bar, for example about 3.8 bar, at the top the second rectification column.
- FIGS. 1 and 2 illustrate air separation plants according to different embodiments of the present invention. Elements that correspond structurally or functionally to one another are indicated in the figures with identical reference symbols and are not explained again for the sake of clarity. Explanations relating to plants and plant components apply in the same way to corresponding processes and process steps.
- FIG. 1 an air separation plant according to an embodiment of the present invention is illustrated in the form of a simplified process flow diagram and is denoted overall by 100 .
- air is sucked in by means of a main air compressor 1 via a filter 2 and compressed to a pressure level of, for example, approximately 12.5 bar.
- a pre-cleaning unit 3 which can be configured in a manner known per se.
- a correspondingly formed stream of compressed air a is passed from the warm to the cold end through a main heat exchanger 4 and fed into a pressure column 11 of a rectification column arrangement 10 .
- the rectification column arrangement 10 has, in addition to the pressure column 11, which has a column jacket 1T, a low-pressure column 12 with a column jacket 12', a two-part crude argon column consisting of the column parts 13a and 13b with column jackets 13a' and 13b', and a pure oxygen column 14 with a column shell 14 'and a pure argon column 15 on.
- the pressure column 11 is connected to the low-pressure column 12 via a main condenser 16 in a heat-exchanging manner, which can be designed in particular as a multi-level bath evaporator, and a bottom evaporator 17 is arranged in the bottom of the pure oxygen column 14 .
- the rectification column system 10 is also assigned a subcooling countercurrent flow device 18 .
- the low-pressure column 12 and the argon column 13a, 13b have rectification areas A to D, a first and second rectification area A, B being provided in the low-pressure column 12 and a first and second rectification area C, D also being provided in the argon column. Between the first and the second rectification region A, B of the low-pressure column 12 is from the An argon-enriched first transfer fluid in the form of a stream t1 is removed from the low-pressure column 12 and fed into the argon column 13a, 13b in a first transfer quantity below the first rectification region C of the argon column 13a, 13b.
- an argon-depleted second transfer fluid is removed from the argon column 13a, 13b in the form of a stream t2 and transferred in a second transfer amount between the first and second rectification region A, B of the low-pressure column 12 into the low-pressure column 12 fed.
- the pure oxygen column 14 is operated with a liquid as reflux, which is withdrawn from the argon column 13a, 13b in the form of a stream r between the first and second rectification regions C, D of the argon column 13a, 13b, and the pure oxygen column 14 produces a top gas in the form taken from a stream g, which is fed into the argon column 13a, 13b between the first and second rectification regions C, D of the argon column 13a, 13b.
- the pressure column 11 and the low-pressure column 12 are connected in a heat-exchanging manner by means of the main condenser 16, with the use of top gas from the low-pressure column 12 forming a circulation stream c, which is passed through the subcooling countercurrent 18, heated in the main heat exchanger 4, compressed by a compressor 5, in the main heat exchanger 4 is cooled again, guided to a part c1 through the main condenser 16 and to a part c2 through the bottom evaporator 17 of the pure oxygen column 14, at least partially condensed there, and fed back into the pressure column 11 and the low-pressure column 12.
- Parts of the top gas of the low-pressure column are branched off from the circuit stream c and discharged in the form of a gas product stream c3 and a liquid product stream c4, the latter being able to be supercooled by expanding a partial stream c5.
- the circuit stream c can also be fed back, in particular substantially completely, into the pressure column 11 without branching off the gas product stream c3 on the hot side of the main heat exchanger 4 after cooling in the main heat exchanger 4, without this being fed through the main condenser 16 and/or beforehand to lead the bottom evaporator 17 of the pure oxygen column 14 .
- the pressure column 11, such as mentioned above, gas, in particular top gas, can be removed above the feed point of the circulating stream c, which gas is further purified in this way compared to the circulating stream c, and this can now be partially or completely passed through the main condenser 16 and/or to a Partly or completely passed through the bottom evaporator 17 of the pure oxygen column 14, at least partially condensed there, and returned to the rectification column arrangement 10.
- the nitrogen product can be provided using overhead gas from the pressure column 11 .
- the first rectification area A and the second rectification area B of the low-pressure column 12 are accommodated in the common column jacket 12', in which the second rectification area B of the low-pressure column 12 is arranged above the first rectification area A of the low-pressure column 12. Furthermore, the first rectification area C of the argon column 13a, 13b is accommodated in the column jacket 13a' and the second rectification area D of the argon column 13a, 13b is accommodated in the separate column jacket 13b'.
- the column jacket 13a' in which the first rectification region C of the argon column 13a, 13b is accommodated, is arranged above the column jacket 14' of the pure oxygen column 14 and is connected to it or formed in one piece with it.
- Bottom liquid is removed from the pressure column in the form of a stream s and, after passing through the supercooling countercurrent 18 and partly used as a heating medium in a bottom evaporator of the pure argon column 15, is fed into liquid baths in the top condensers of the argon column 13a, 13b and the pure argon column 15.
- Gas formed there and corresponding purge quantities are fed into the low-pressure column 12 in the form of streams s1 to s3.
- Gas from above the first rectification area C of the argon column 13a, 13b and top gas of the pure oxygen column g is, as already partially mentioned, transferred below the second rectification area D into the corresponding part 13b of the argon column 13a, 13b.
- resulting sump liquid is by means of a pump 18 upwards of the first rectification area A into the corresponding part 13a of the argon column 13a, 13b and, as mentioned, into the pure oxygen column 14.
- the argon column 13a, 13b designed here as a crude argon column and the pure argon column 15 are operated in the manner known in principle from the field of argon production. Reference is therefore made to the relevant specialist literature.
- a pure argon stream p is withdrawn in liquid form from the pure argon column 15, which is internally compressed and discharged as a gaseous argon pressure product.
- a pure oxygen stream o liquid is withdrawn from the bottom of the pure oxygen column 14 and can be stored, for example, in a tank system (not shown).
- a gas stream t can be drawn off from the low-pressure column 12 below the first rectification region A, subjected to any dilution gas stream v, heated in the main heat exchanger 8, expanded to an intermediate temperature by means of a residual gas turbine 8 braked, for example, by a generator G and discharged or heated to the atmosphere and in the pre-cleaning unit 3.
- pure oxygen can be vaporized in the main heat exchanger and released as a corresponding pure oxygen product.
- FIG. 2 illustrates an air separation plant 200 according to a further embodiment of the invention in a simplified representation.
- the first rectification area A of the low-pressure column 12a, 12b is accommodated in a first column jacket 12a'
- the second rectification area B of the low-pressure column 12a, 12b is accommodated in a second column jacket 12b'
- the first and the second column jacket 12a', 12b' are arranged side by side.
- the first column jacket 12a' and the column jacket 1T of the pressure column 11 are arranged one above the other and are designed in the form of a double column.
- the second rectification area D of the argon column 13a, 13b is divided into a first partial area D1 and a second Section D2 divided, with the first rectification section C of the argon column 13a, 13b being housed in a third column jacket 13a', the first section D1 of the second rectification section D of the argon column 13a, 13b above the first rectification section C of the argon column 13a, 13b in the third column jacket 13a' is accommodated, and the second partial area D1 of the second rectification area D of the argon column 13a, 13b is accommodated in the fourth column jacket 13b'.
- gas is withdrawn from the first column jacket 12a' in the form of a stream k above the first rectification region A of the low-pressure column 12a, 12b and in a first proportion in the form of a stream k1 below the second rectification region B of the low-pressure column 12a, 12b into the second column jacket 12b' and in a second proportion in the form of a stream k2 below the first rectification region C of the argon column 13a, 13b as the first transfer fluid into the third column jacket 13b'.
- Liquid is withdrawn in the form of a stream m from the third column jacket 13b' below the first rectification region C of the argon column 13a, 13b and is fed into the first column jacket 12a' above the first rectification region A of the low-pressure column 12a, 12b as the second transfer fluid, and liquid is fed in the form of a stream n below the second rectification area B of the low-pressure column 12a, 12b from the second column jacket 12b' and fed below the first rectification area C of the argon column 13a, 13b into the third column jacket 13a'.
- a lower end of the second column jacket 12b' is arranged geodetically above a feeding position of the first transfer fluid into the third column jacket 13a', so that the first transfer fluid is transferred into the third column jacket 13a' purely by gravity.
- the pure oxygen column 14 is operated with a liquid as reflux, which is withdrawn from the argon column 13a, 13b in the form of a stream r between the first and second rectification regions C, D of the argon column 13a, 13b, and the pure oxygen column 14 produces a top gas in the form taken from a stream g, which is fed into the argon column 13a, 13b between the first and second rectification regions C, D of the argon column 13a, 13b.
- a liquid as reflux which is withdrawn from the argon column 13a, 13b in the form of a stream r between the first and second rectification regions C, D of the argon column 13a, 13b
- the pure oxygen column 14 produces a top gas in the form taken from a stream g, which is fed into the argon column 13a, 13b between the first and second rectification regions C, D of the argon column 13a, 13b.
- Air separation plant 100 according to FIG. 1 and air separation plant 200 according to FIG is discharged from the air separation plant 100, 200 in the form of a material flow c3 in the first operating mode, and in the second operating mode the first transfer quantity of the material flow t1 or k2, i.e. the first transfer fluid, is set to a lower value than in the first operating mode.
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- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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CN202280063915.XA CN117980677A (zh) | 2021-09-01 | 2022-08-24 | 用于空气低温分离的方法和空气分离设备 |
KR1020247010075A KR20240059619A (ko) | 2021-09-01 | 2022-08-24 | 공기의 저온 분리 방법 및 공기 분리 플랜트 |
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EP21020438 | 2021-09-01 | ||
EP21020438.4 | 2021-09-01 |
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WO2023030679A1 true WO2023030679A1 (de) | 2023-03-09 |
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PCT/EP2022/025388 WO2023030679A1 (de) | 2021-09-01 | 2022-08-24 | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage |
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KR (1) | KR20240059619A (de) |
CN (1) | CN117980677A (de) |
TW (1) | TW202311682A (de) |
WO (1) | WO2023030679A1 (de) |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5255524A (en) * | 1992-02-13 | 1993-10-26 | Air Products & Chemicals, Inc. | Dual heat pump cycles for increased argon recovery |
JPH0835768A (ja) * | 1994-07-22 | 1996-02-06 | Hitachi Ltd | 空気分離装置 |
US6543253B1 (en) * | 2002-05-24 | 2003-04-08 | Praxair Technology, Inc. | Method for providing refrigeration to a cryogenic rectification plant |
EP3327393A1 (de) * | 2016-11-25 | 2018-05-30 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung eines hochreinsauerstoffproduktstroms durch tieftemperaturzerlegung von luft |
DE202021000696U1 (de) * | 2021-02-16 | 2021-08-18 | Linde Gmbh | Bereitstellung eines Stickstoffprodukts |
WO2022058043A1 (en) * | 2020-09-17 | 2022-03-24 | Linde Gmbh | Process and apparatus for cryogenic separation of air with mixed gas turbine |
-
2022
- 2022-08-24 WO PCT/EP2022/025388 patent/WO2023030679A1/de active Application Filing
- 2022-08-24 CN CN202280063915.XA patent/CN117980677A/zh active Pending
- 2022-08-24 KR KR1020247010075A patent/KR20240059619A/ko unknown
- 2022-08-29 TW TW111132399A patent/TW202311682A/zh unknown
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5255524A (en) * | 1992-02-13 | 1993-10-26 | Air Products & Chemicals, Inc. | Dual heat pump cycles for increased argon recovery |
JPH0835768A (ja) * | 1994-07-22 | 1996-02-06 | Hitachi Ltd | 空気分離装置 |
US6543253B1 (en) * | 2002-05-24 | 2003-04-08 | Praxair Technology, Inc. | Method for providing refrigeration to a cryogenic rectification plant |
EP3327393A1 (de) * | 2016-11-25 | 2018-05-30 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung eines hochreinsauerstoffproduktstroms durch tieftemperaturzerlegung von luft |
WO2022058043A1 (en) * | 2020-09-17 | 2022-03-24 | Linde Gmbh | Process and apparatus for cryogenic separation of air with mixed gas turbine |
DE202021000696U1 (de) * | 2021-02-16 | 2021-08-18 | Linde Gmbh | Bereitstellung eines Stickstoffprodukts |
Non-Patent Citations (1)
Title |
---|
"Industrial Gases Processing", 2006, WILEY-VCH |
Also Published As
Publication number | Publication date |
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CN117980677A (zh) | 2024-05-03 |
TW202311682A (zh) | 2023-03-16 |
KR20240059619A (ko) | 2024-05-07 |
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