WO2022214214A1 - Verfahren und anlage zur tieftemperaturzerlegung von luft - Google Patents
Verfahren und anlage zur tieftemperaturzerlegung von luft Download PDFInfo
- Publication number
- WO2022214214A1 WO2022214214A1 PCT/EP2022/025098 EP2022025098W WO2022214214A1 WO 2022214214 A1 WO2022214214 A1 WO 2022214214A1 EP 2022025098 W EP2022025098 W EP 2022025098W WO 2022214214 A1 WO2022214214 A1 WO 2022214214A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- rectification column
- stream
- pressure level
- condenser
- fed
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 54
- 238000005194 fractionation Methods 0.000 title abstract 2
- 239000007788 liquid Substances 0.000 claims abstract description 71
- 239000007789 gas Substances 0.000 claims abstract description 53
- 239000001301 oxygen Substances 0.000 claims abstract description 46
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 46
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract 10
- 238000000926 separation method Methods 0.000 claims description 58
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 48
- 238000001704 evaporation Methods 0.000 claims description 36
- 230000008020 evaporation Effects 0.000 claims description 29
- 229910052757 nitrogen Inorganic materials 0.000 claims description 24
- 239000000463 material Substances 0.000 claims description 21
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 12
- 229910052786 argon Inorganic materials 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 2
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 238000011144 upstream manufacturing Methods 0.000 claims 1
- 238000001228 spectrum Methods 0.000 abstract description 17
- 238000009833 condensation Methods 0.000 abstract description 10
- 230000005494 condensation Effects 0.000 abstract description 10
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 40
- 239000012530 fluid Substances 0.000 description 23
- 238000001816 cooling Methods 0.000 description 6
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000001419 dependent effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229910052743 krypton Inorganic materials 0.000 description 1
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 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
- 238000000746 purification Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
-
- 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
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
-
- 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
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
-
- 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
-
- 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
- F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
-
- 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
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
-
- 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
-
- 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
- F25J3/04309—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 nitrogen
- F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
-
- 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
-
- 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
- F25J3/04406—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 using a dual pressure main column system
- F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
-
- 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
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
-
- 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
-
- 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
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
-
- 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
-
- 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
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/04—Multiple expansion turbines in parallel
-
- 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
-
- 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
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
-
- 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 invention relates to a method for the low-temperature separation of air and a corresponding system according to the preambles of the independent patent claims.
- Air separation plants have rectification column systems which can be conventionally designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three- or multi-column systems.
- rectification columns for obtaining nitrogen and/or oxygen in a liquid and/or gaseous state i.e. the rectification columns for nitrogen-oxygen separation
- rectification columns for obtaining further air components in particular the noble gases krypton, xenon and/or argon.
- the terms “rectification” and “distillation” as well as “column” and “column” or terms composed of these are often used synonymously.
- the rectification columns of the rectification column systems mentioned are operated at different pressure levels.
- Known double column systems have a so-called high-pressure column (also referred to as a pressure column, medium-pressure column or lower column) and a so-called low-pressure column (also referred to as an upper column).
- the high-pressure column is typically operated at a pressure level of 4 to 7 bar, in particular about 5.3 bar.
- the low-pressure column is operated at a pressure level of typically 1 to 2 bar, in particular about 1.4 bar. In certain cases, higher pressure levels can also be used in both rectification columns.
- the pressures given below are absolute pressures at the top of the columns given in each case.
- the object of the present invention is to improve a SPECTRA process with corresponding oxygen generation, primarily with regard to energy consumption and material yield.
- Liquids and gases can be rich or poor in one or more components, with “rich” meaning at least 75%, 90%, 95%, 99%, 99.5%, 99.9% or 99.99% and “poor” for one content of at most 25%, 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis.
- the term “predominantly” may correspond to the definition of "rich”.
- Liquids and gases can also be enriched or depleted in one or more components, these terms referring to a content in a starting liquid or a starting gas from which the liquid or gas was obtained.
- the liquid or the gas is "enriched” if this or this at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times, 100 times or 1,000 times the content, and " depleted” if it contains at most 0.9, 0, 5, 0.1, 0.01 or 0.001 times the content of a corresponding component, based on the starting liquid or the starting gas . If, for example, “oxygen”, “nitrogen” or “argon” is mentioned here, this also includes a liquid or a gas that is rich in oxygen or nitrogen, but does not have to consist exclusively of them.
- turboexpanders typically known turboexpanders are understood. These expansion machines can in particular also be coupled with compressors. These compressors can in particular be turbo compressors.
- a corresponding combination of turboexpander and turbocompressor is typically also referred to as a "turbine booster". In a turbine booster are the turbo expander and the turbo compressor mechanically coupled, the coupling can be done at the same speed (e.g. via a common shaft) or at different speeds (e.g. via a suitable translating gear).
- compressor is generally used here.
- a "cold compressor” refers here to a compressor to which a fluid flow at a temperature level well below 0 °C, in particular below -50, -75 or -100 °C and up to -150 or -200 °C is supplied. A corresponding fluid flow is cooled to a corresponding temperature level in particular by means of a Flaupt heat exchanger (see below).
- Such a heat exchanger has "passages” which are designed as separate fluid channels with heat exchange surfaces and are joined together in parallel and separated by other passages to form “passage groups". hallmark of one Heat exchanger is that heat is exchanged between two mobile media in it at a time, namely at least one fluid stream to be cooled and at least one fluid stream to be heated.
- a “condenser evaporator” is a heat exchanger in which a condensing fluid stream enters into indirect heat exchange with an 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 condensing fluid flow is carried out in the liquefaction space, and the evaporation of the evaporating fluid flow is carried out in the evaporation space.
- the evaporating and condensing spaces are formed by groups of passages which are in heat exchange relationship with each other.
- a “condenser evaporator assembly” as used herein may include one or more condenser evaporators.
- a condenser evaporator of a condenser evaporator arrangement can be designed for use in the present invention, for example, as a so-called bath evaporator well known to the person skilled in the art.
- a so-called “forced flow” condenser evaporator can also be used, in which a liquid or two-phase flow is forced through the evaporation space by its own pressure and is partially or completely evaporated there. This pressure can be generated, for example, by a liquid column in the feed line to the evaporation space. The fleas of this liquid column corresponds to the pressure loss in the evaporation space.
- the present invention comprises the low-temperature decomposition of air according to the so-called SPECTRA method, as described, inter alia, in EP 2 789 958 A1 and the other patent literature cited there. In the simplest embodiment, this is a single-column process. However, this is not the case in the context of the present invention, because here, in addition to an air-fed rectification column ("first" rectification column), one from the first Rectification column fed and used for oxygen recovery rectification column (“second" rectification column) is used.
- first air-fed rectification column
- second oxygen recovery rectification column
- a reflux from the first rectification column used for this purpose is provided by condensing top gas from the first rectification column, more precisely part of this top gas, in a heat exchanger.
- a condenser-evaporator which is part of a corresponding condenser-evaporator arrangement (here as "first"
- Condenser-evaporator arrangement referred to
- fluid which is also removed from the first rectification column, used for cooling and thereby evaporated or partially evaporated.
- Additional overhead gas can be provided as a nitrogen-rich product.
- a corresponding condenser-evaporator arrangement can have one or more condenser-evaporators.
- first and second streams are formed in the first condenser-evaporator arrangement with the evaporation of liquid from the first rectification column, with the first stream in one embodiment of the invention using liquid is formed, which is taken from the first rectification column with a first oxygen content, and the second stream is formed using liquid which is taken from the first rectification column with a second, higher oxygen content.
- the liquid used in the stream can be drawn off from the first rectification column from an intermediate tray or from a liquid retention device.
- the liquid used to form the second stream can in particular be at least part of the liquid bottom product of the first rectification column.
- the same liquid can also initially be used to form the first and the second stream, for example bottom liquid from the first rectification column or another liquid taken from the first rectification column.
- This can be passed through the first condenser-evaporator arrangement, partially evaporated in the process, and subjected to phase separation to obtain a gas fraction and a liquid fraction.
- the first stream can be formed with the first oxygen content using the gas fraction or a part thereof.
- the condenser-evaporator arrangement can have only one condenser-evaporator.
- the second material flow can be formed by evaporating the liquid fraction or a part thereof in one condenser-evaporator of the first condenser-evaporator arrangement.
- the first and second streams are fluids that are used beforehand in the first condenser-evaporator arrangement for cooling and for condensing the corresponding portion of overhead gas from the first rectification column.
- the bottom liquid of the first rectification column can first be passed through a condenser-evaporator of the first condenser-evaporator arrangement, being partially evaporated in the process, and subjected to phase separation to obtain a gas fraction and a liquid fraction.
- the first stream can be formed with the first oxygen content using the gas fraction or a part thereof.
- the liquid remaining after the first evaporation is fed into another condenser-evaporator of the first condenser-evaporator arrangement and is completely or almost completely evaporated there.
- the second stream can in this Configuration are formed thereof by evaporation of this liquid or a part.
- the first condenser-evaporator arrangement can therefore be divided practically into two smaller units, which are preferably connected in parallel on the condensation side.
- the first stream can be compressed at least in part by means of a cold compressor after it has been used for cooling in the first condenser-evaporator arrangement and returned to the first rectification column.
- a cold compressor after it has been used for cooling in the first condenser-evaporator arrangement, the second material flow can be at least partially expanded and carried out as a so-called residual gas mixture from the air separation plant.
- one or more compressors can be used, which is or are coupled to one or more expansion machines, in which the expansion of the second material flow (or a corresponding part) is made.
- a compressor can be used here that is coupled to one of two expansion machines arranged in parallel. If only one expander is used, the compressor can be coupled to it.
- the wording used below for reasons of clarity, according to which "a" compressor is coupled to "an” expansion machine, does not exclude the use of a plurality of compressors and/or expansion machines in any mutual coupling.
- the described compressor or compressors do not have to be driven, in particular not exclusively, by means of the one or more expansion machines mentioned.
- the compressor or compressors do not have to take up all of the work released during expansion.
- assisted or exclusive drive may also be provided using an electric motor, or generator and/or oil brakes may be provided in any arrangement.
- the compressor or compressors are one or more cold compressors, since the first fluid stream is fed to this or these despite its routing through the first condenser evaporator arrangement and any subsequent further heating at a low temperature level.
- second condenser/evaporator arrangement in the lower region of the second rectification column which is used for reboiling bottoms liquid from the second rectification column.
- the reason for the high specific energy requirement is mainly that the explained "heating" in the mentioned second condenser-evaporator arrangement in the lower area of the second rectification column is realized to a large extent by the mentioned condensing part of the gaseous feed air.
- This The (liquefied) partial air flow is then (after its evaporation) used to generate refrigeration capacity or to drive the cold compressor or compressors used by taking a corresponding amount of fluid as a second material flow from the first rectification column, but this no longer takes part in the rectification process part of the first rectification column.
- a method of the type explained above can be modified in an embodiment not according to the invention in that instead of a feed air stream in the second condenser-evaporator arrangement in the lower region of the second rectification column, fluid is used which, in the manner explained above, is part of the "first" or "second" Material flow in the first
- Condenser evaporator assembly was evaporated. In this way, one can save the air previously used for this purpose, thereby increasing energy efficiency and yield. The condensed fluid can then be treated as discussed below.
- the condensation in the second condenser-evaporator arrangement can be carried out at a pressure level at which the evaporation of the corresponding fluid was previously carried out in the first condenser-evaporator arrangement.
- the condensed gas or the condensate formed can be brought to the required pressure by means of a pump.
- the operation of a pump is significantly more reliable and its provision is significantly cheaper. Nevertheless, an operation without a corresponding pump is to be aimed at.
- the present invention ensures this.
- the operating pressure of the second rectification column can also be so high that energy can be recovered from its top gas by, according to the invention, using it from the turbine stream the first condenser-evaporator arrangement (the second material stream) is admixed.
- the corresponding current was simply throttled, causing a great loss of energy.
- the present invention proposes, in the language of the patent claims, a method for the low-temperature separation of air, in which an air separation plant with a first rectification column and a second rectification column is used.
- the first rectification column is operated at a first pressure level and the second rectification column is operated at a second pressure level below the first pressure level.
- first and second pressure levels are higher pressure levels than are used in conventional air separation plants, in particular SPECTRA plants with oxygen recovery.
- the first pressure level can be in particular 7 to 14 bar, the second pressure level in particular 4 to 7 bar.
- These are absolute pressures at the top of the respective rectification columns.
- the first rectification column and the second rectification column can, in particular, be arranged next to one another and are typically not combined with one another in the form of a double column, with a "double column” generally being understood here to mean a separating apparatus formed from two rectification columns, which is designed as a structural unit in which the column jackets of the two rectification columns are connected to one another without a line, i.e. directly, in particular by welding. However, this direct connection alone does not have to establish a fluidic connection.
- Atmospheric air which was compressed and then cooled, is fed to the first rectification column.
- appropriate air can be fed to the first rectification column in the form of a plurality of streams, which can be treated differently and, if appropriate, passed through other apparatus beforehand.
- no air is typically fed to the second rectification column.
- the second rectification column is fed from the first rectification column, or the second rectification column is typically not fed with streams which have not previously been removed from the first rectification column or formed from such streams.
- first rectification column overhead gas is recovered as nitrogen product and discharged from the air separation unit
- second rectification column bottoms is recovered as oxygen product and discharged from the air separation unit. This does not preclude other fluids from being discharged from the air separation plant and released into the atmosphere, for example. Certain parts of fluids otherwise discharged as nitrogen or oxygen product can also be discharged in the context of the present invention, for example as purge streams or as a further liquid nitrogen product after condensation of overhead gas from the first rectification column.
- a first and a second stream are formed within the scope of the present invention by evaporating liquid from the first rectification column, with the evaporation in particular comprising two evaporation steps carried out separately below the first pressure level at the same or different evaporation pressures.
- the evaporation pressures in the first condenser-evaporator arrangement are in particular between 3.5 and 7.5 bara (bar absolute pressure, the values can represent exact or approximate values) and are dependent on the first pressure level. Therefore, the fluid to be evaporated here, which was taken from the first rectification column, is expanded accordingly.
- More head gas of the first rectification column which is not provided as a gaseous nitrogen product, is condensed in the first condenser-evaporator arrangement and returned to the first rectification column as reflux.
- a proportion of the corresponding condensate can also be discharged as the further liquid nitrogen product mentioned, in particular after supercooling against itself.
- the first stream or a part thereof is partially or completely subjected to recompression to the first pressure level and fed into the first rectification column, and the second stream or a part thereof is subjected to expansion and discharged from the air separation plant.
- the second rectification column is equipped with the second condenser-evaporator arrangement or at least thermally coupled to it, the second condenser-evaporator arrangement being in particular in a bottom region of the second Rectification column is formed or provided and is in particular partially submerged in a forming in the bottom area liquid bath.
- the bottom liquid of the second rectification column is evaporated in the second condenser-evaporator arrangement.
- the advantage of the interconnection provided according to the invention consists in particular in the fact that a total of up to approx. 4.7% less input air (or accordingly approx. 4.7% less energy) is required to obtain the same products 29,300 standard cubic meters per hour of compressed nitrogen (PGAN) under approx. 11 bara and 700 standard cubic meters per hour of high-purity liquid oxygen (UHPLOX) can be provided.
- GPN compressed nitrogen
- UHPLOX high-purity liquid oxygen
- a particular further advantage of the present invention is that for the return of the formed in the second condenser-evaporator assembly Condensate no pump is required and thus the investment and operating costs can be reduced and the system is easier to maintain.
- Two alternatives of the invention relate in particular to the specific type of partial condensation of the first stream or of its part which is subjected to recompression to the first pressure level and is fed into the first rectification column.
- the first material stream or the part thereof that is subjected to recompression to the first pressure level and is fed into the first rectification column is led to a first portion through the second condenser-evaporator arrangement, in which at least a predominant portion, in particular completely, liquefied and fed into the first rectification column, and the first material stream or part thereof which is subjected to recompression to the first pressure level and fed into the first rectification column is fed into the first rectification column in a second proportion unliquefied, without being fed through the second To be performed condenser evaporator assembly.
- the first stream or the part thereof that is subjected to recompression to the first pressure level and is fed into the first rectification column is passed through the second
- Condenser-evaporator arrangement out, but only partially liquefied in this, and fed in the form of a two-phase stream, the first rectification column.
- the two-phase stream can in particular have a steam content of 0.7 to 0.95, for example approx. 0.8, in molar proportions and based on its total amount.
- the feeding of the first stream or the part thereof that is subjected to recompression to the first pressure level and fed into the first rectification column, or the liquid and gaseous fraction after partial liquefaction, can be fed in at least in part into a lower region of the first rectification column take place.
- a "lower area" can be a position below which there are no longer any separating devices such as sieve trays or packings in the first rectification column.
- the compressed nitrogen product from the first rectification column could also be used to heat the second condenser-evaporator arrangement and subjected to a corresponding condensation.
- the first stream or the part thereof that is subjected to recompression to the first pressure level and is fed into the first rectification column is brought to a third pressure level in particular during recompression, which corresponds at least to the first pressure level, with the partial liquefaction taking place in particular on the first pressure level minus pressure losses in the main heat exchanger and the connecting lines.
- a particular advantage of the invention is that the first stream or the part thereof that is subjected to recompression to the first pressure level and is fed into the first rectification column, or the liquid and gaseous fractions, is or are transferred without a pump into the first rectification column.
- one or more compressors can also be provided within the scope of the present invention for the recompression of the first stream or that part thereof which is subjected to recompression to the first pressure level and fed into the first rectification column be, and for the work-expansion of the second stream or the part thereof, which is subjected to the work-expansion and discharged from the air separation plant, one or more expansion machines can be provided, which is or are coupled to the one or more compressors . Further details have already been explained in general above for SPECTRA methods.
- the process of the present invention can recover a first rectification column overhead gas, and hence a nitrogen product, containing less than 1 ppb each of oxygen, carbon monoxide and/or hydrogen and less than 10 ppm argon on a volume basis.
- the bottoms liquid of the second rectification column may contain less than 10 ppb argon and/or 5 ppm methane on a volume basis and otherwise consist essentially of oxygen.
- none of the cooled compressed air to be separated in the process is liquefied, or only to a small extent, and is therefore fed into the first rectification column in at least a predominantly gaseous state.
- the air separation plant is also set up to form the first stream with a first oxygen content and the second stream with a second oxygen content above the first oxygen content, to subject the first stream or a part thereof to recompression to the first pressure level and to feed it into the first rectification column , and to subject the second stream or a part thereof to expansion and discharge it from the air separation plant, and to evaporate bottom liquid of the second rectification column in the second condenser-evaporator arrangement.
- means are provided which are set up to at least to subject part of a partial liquefaction in the second condenser-evaporator arrangement and to feed it in the form of a two-phase stream into the first rectification column and to supply top gas of the second rectification column to a work-expansion expansion.
- FIG. 1 shows an air separation plant according to an embodiment of the invention.
- FIG. 3 shows an air separation plant according to an embodiment of the invention.
- FIG. 1 shows an air separation plant 100 in the form of a schematic plant diagram.
- the central component is a rectification column system 10 with a first rectification column 11, a second rectification column 12, a first condenser evaporator 111 and a second condenser evaporator 121.
- the first rectification column 11 is operated at a first pressure level
- the second rectification column 12 is operated at a second pressure level below the first pressure levels operated.
- the first and second condenser evaporators 111 and 121 may each be part of a first and second condenser evaporator assembly, respectively.
- a first and a second condenser evaporator 111 , 121 are mentioned below merely for the sake of clarity.
- a pilot air compressor 1 of the air separation plant 100 By means of a pilot air compressor 1 of the air separation plant 100, air is sucked in from the atmosphere A and compressed via a filter that is not designated separately. After cooling in an aftercooler, also not designated separately, downstream of the main air compressor 1, the feed air stream a formed in this way is further cooled in a direct contact cooler 2 operated with water W. The feed air stream a is then subjected to purification in an adsorber unit 3.
- an adsorber unit 3 for further explanations in this context, reference is made to the specialist literature, for example in connection with FIG. 2.3A in Häring (see above). After cooling in the main heat exchanger 4, the feed air stream a is fed into the first rectification column 11.
- part of the feed air stream a would be fed into the first rectification column 11, while another part would be passed through the second condenser evaporator 121, which is in a lower Area of the second rectification column 12 is arranged, and by means of which the bottom liquid of the second rectification column 12 is evaporated. This further part would be partially condensed in the second condenser-evaporator 121 and then also fed into the first rectification column 11 .
- Top gas of the first rectification column 11 is discharged from the air separation plant 100 in the form of a stream d as nitrogen product B or dense gas C.
- Bottom liquid from the second rectification column 12, on the other hand, is discharged as oxygen product D in the form of a stream e. It is also possible, for example, to feed what are known as run tanks for later evaporation to provide an internally compressed oxygen product D.
- a first material flow g and a second material flow h are subjected to evaporation below the first pressure level (for this purpose, in particular, a corresponding expansion takes place in valves that are not designated separately).
- Additional top gas from the first rectification column 11 is condensed in the form of a stream i in the first condenser-evaporator 111 and returned to the first rectification column 11 as reflux.
- a portion can also be supercooled in a supercooler 5 and made available as liquid nitrogen F, as illustrated here in the form of a stream k.
- a material flow I that is heated in the process is treated as explained in more detail below.
- a further discharge in the form of a purge flow m or P can also be provided.
- a possible injection of liquid nitrogen (LIN injection) is denoted by Q.
- gas of the second stream h is partially expanded via a throttle 9 in the example illustrated here, then combined with top gas, which is drawn off in the form of a stream o from the second rectification column 12, a parallel further expansion subjected to expansion machines 7 and 8 and, after heating in the Flaupt heat exchanger 4, used as regeneration gas in the adsorber unit 3 or released into the atmosphere A and thus discharged from the air separation plant 100.
- the expansion machine 7 is coupled to the compressor 6, the expansion machine 8 to a generator G.
- a different number of corresponding machines or a different type of coupling can also be used in each case.
- An unspecified (oil) brake can also be provided.
- the second rectification column 12 is fed with a side stream p from the first rectification column 11, which is fed to the second rectification column in an upper region. Furthermore, a first portion of the first material flow g or a corresponding part thereof is conducted through the second condenser-evaporator 121 after its evaporation or partial evaporation in the first condenser-evaporator 111 and after its recompression in the compressor 6 as a partial flow b and subjected to partial condensation. Correspondingly formed liquid or two-phase mixture, further denoted by b, is transferred into the first rectification column 11 without a pump.
Landscapes
- Engineering & Computer Science (AREA)
- 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 (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US18/554,396 US20240183610A1 (en) | 2021-04-09 | 2022-03-10 | Method and plant for low temperature fractionation of air |
KR1020237037721A KR20230171441A (ko) | 2021-04-09 | 2022-03-10 | 공기의 저온 분리를 위한 방법 및 플랜트 |
EP22711877.5A EP4320397A1 (de) | 2021-04-09 | 2022-03-10 | Verfahren und anlage zur tieftemperaturzerlegung von luft |
CN202280027076.6A CN117157498A (zh) | 2021-04-09 | 2022-03-10 | 用于低温分离空气的方法和设备 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP21020190.1 | 2021-04-09 | ||
EP21020190 | 2021-04-09 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2022214214A1 true WO2022214214A1 (de) | 2022-10-13 |
Family
ID=75674599
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2022/025098 WO2022214214A1 (de) | 2021-04-09 | 2022-03-10 | Verfahren und anlage zur tieftemperaturzerlegung von luft |
Country Status (6)
Country | Link |
---|---|
US (1) | US20240183610A1 (de) |
EP (1) | EP4320397A1 (de) |
KR (1) | KR20230171441A (de) |
CN (1) | CN117157498A (de) |
TW (1) | TW202240115A (de) |
WO (1) | WO2022214214A1 (de) |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4783210A (en) * | 1987-12-14 | 1988-11-08 | Air Products And Chemicals, Inc. | Air separation process with modified single distillation column nitrogen generator |
JP2917031B2 (ja) * | 1989-09-12 | 1999-07-12 | 日本酸素株式会社 | 酸素の製造方法 |
US6279345B1 (en) * | 2000-05-18 | 2001-08-28 | Praxair Technology, Inc. | Cryogenic air separation system with split kettle recycle |
JP2004020158A (ja) * | 2002-06-20 | 2004-01-22 | Air Water Inc | 空気分離装置 |
EP1995537A2 (de) * | 2007-05-24 | 2008-11-26 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung |
EP2789958A1 (de) | 2013-04-10 | 2014-10-15 | Linde Aktiengesellschaft | Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage |
WO2021104668A1 (de) * | 2019-11-26 | 2021-06-03 | Linde Gmbh | Verfahren und anlage zur tieftemperaturzerlegung von luft |
-
2022
- 2022-03-10 WO PCT/EP2022/025098 patent/WO2022214214A1/de active Application Filing
- 2022-03-10 CN CN202280027076.6A patent/CN117157498A/zh active Pending
- 2022-03-10 KR KR1020237037721A patent/KR20230171441A/ko unknown
- 2022-03-10 US US18/554,396 patent/US20240183610A1/en active Pending
- 2022-03-10 EP EP22711877.5A patent/EP4320397A1/de active Pending
- 2022-04-06 TW TW111113005A patent/TW202240115A/zh unknown
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4783210A (en) * | 1987-12-14 | 1988-11-08 | Air Products And Chemicals, Inc. | Air separation process with modified single distillation column nitrogen generator |
JP2917031B2 (ja) * | 1989-09-12 | 1999-07-12 | 日本酸素株式会社 | 酸素の製造方法 |
US6279345B1 (en) * | 2000-05-18 | 2001-08-28 | Praxair Technology, Inc. | Cryogenic air separation system with split kettle recycle |
JP2004020158A (ja) * | 2002-06-20 | 2004-01-22 | Air Water Inc | 空気分離装置 |
EP1995537A2 (de) * | 2007-05-24 | 2008-11-26 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung |
EP2789958A1 (de) | 2013-04-10 | 2014-10-15 | Linde Aktiengesellschaft | Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage |
WO2021104668A1 (de) * | 2019-11-26 | 2021-06-03 | Linde Gmbh | Verfahren und anlage zur tieftemperaturzerlegung von luft |
Non-Patent Citations (1)
Title |
---|
"Industrial Gases Processing", 2006, WILEY-VCH |
Also Published As
Publication number | Publication date |
---|---|
US20240183610A1 (en) | 2024-06-06 |
EP4320397A1 (de) | 2024-02-14 |
TW202240115A (zh) | 2022-10-16 |
KR20230171441A (ko) | 2023-12-20 |
CN117157498A (zh) | 2023-12-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP2235460B1 (de) | Verfahren und vorrichtung zur tieftemperatur-luftzerlegung | |
EP1357342B1 (de) | Drei-Säulen-System zur Tieftemperaturzerlegung mit Argongewinnung | |
EP1067345B1 (de) | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft | |
EP3410050B1 (de) | Verfahren zur gewinnung eines oder mehrerer luftprodukte und luftzerlegungsanlage | |
EP2026024A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft | |
EP1482266A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft | |
EP2236964A1 (de) | Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung | |
WO2020169257A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
EP3870915A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
EP2520886A1 (de) | Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft | |
DE102007035619A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft | |
EP4065910A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
WO2021078405A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
EP3980705A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
EP2551619A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff und Drucksauerstoff durch Tieftemperaturzerlegung von Luft | |
EP2914913B1 (de) | Verfahren zur tieftemperaturzerlegung von luft in einer luftzerlegungsanlage und luftzerlegungsanlage | |
EP1750074A1 (de) | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft | |
DE19933558C5 (de) | Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft | |
EP3557166A1 (de) | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage | |
EP4133227A2 (de) | Verfahren zur tieftemperaturzerlegung von luft, luftzerlegungsanlage und verbund aus wenigstens zwei luftzerlegungsanlagen | |
DE102017010001A1 (de) | Verfahren und Anlage zur Tieftemperaturzerlegung von Luft | |
WO2022214214A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
WO2020187449A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
EP2963371B1 (de) | Verfahren und vorrichtung zur gewinnung eines druckgasprodukts durch tieftemperaturzerlegung von luft | |
EP3870917B1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 22711877 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 18554396 Country of ref document: US |
|
ENP | Entry into the national phase |
Ref document number: 20237037721 Country of ref document: KR Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1020237037721 Country of ref document: KR |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2022711877 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 2022711877 Country of ref document: EP Effective date: 20231109 |