EP4211409A1 - Procédé d'obtention d'un ou de plusieurs produits à base d'air, et installation de fractionnement d'air - Google Patents

Procédé d'obtention d'un ou de plusieurs produits à base d'air, et installation de fractionnement d'air

Info

Publication number
EP4211409A1
EP4211409A1 EP21751977.6A EP21751977A EP4211409A1 EP 4211409 A1 EP4211409 A1 EP 4211409A1 EP 21751977 A EP21751977 A EP 21751977A EP 4211409 A1 EP4211409 A1 EP 4211409A1
Authority
EP
European Patent Office
Prior art keywords
air
pressure
column
fed
pressure level
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP21751977.6A
Other languages
German (de)
English (en)
Inventor
Daniel Palaniswamy OTTE
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP4211409A1 publication Critical patent/EP4211409A1/fr
Pending legal-status Critical Current

Links

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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • 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
    • F25J3/04084—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 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
    • 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
    • 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
    • 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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • 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
    • 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.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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
    • F25J3/04406—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
    • F25J3/04412—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 in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • 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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of 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
    • 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
    • F25J2215/54—Oxygen production with multiple pressure O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid 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
    • 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

Definitions

  • the present invention relates to a method for obtaining one or more air products and an air separation plant according to the respective preambles of the independent patent claims.
  • Air separation plants of the classic type have column systems which can be designed, for example, as two-column systems, in particular as double-column systems, but also as three- or multi-column systems.
  • rectification columns for obtaining nitrogen and/or oxygen in the liquid and/or gaseous state ie rectification columns for nitrogen-oxygen separation, rectification columns for obtaining further air components, in particular inert gases, can be provided.
  • the rectification columns of the column systems mentioned are operated at different pressure levels.
  • Known double column systems 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 5.6 bar, while 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 specified here and below are absolute pressures at the top of the columns specified in each case.
  • the object of the present invention is to improve methods for the low-temperature decomposition of air and for the provision of air products and, in particular, to design them in an energetically more favorable manner.
  • So-called main (air) compressor/boost compressor main air compressor/booster air compressor, MAC-BAC) method or so-called high air pressure (HAP) method can be used for air separation.
  • the main air compressor/boosting processes are the more conventional processes, high air pressure processes are increasingly being used as alternatives in recent times.
  • Main air compressor/post-compressor processes are characterized in that only part of the total amount of feed air supplied to the column system is compressed to a pressure level that is significantly, ie at least 3, 4, 5, 6, 7, 8, 9 or 10 bar above of the pressure level of the pressure column, and thus the highest pressure level used in the column system. A further portion of the feed air quantity is only compressed to the pressure level of the pressure column or a pressure level which differs therefrom by no more than 1 to 2 bar and is fed into the pressure column at this pressure level without expansion.
  • An example of such a main air compressor/post-compressor process is shown by Häring (see above) in Figure 2.3A.
  • the total amount of feed air fed to the column system is compressed to a pressure level which is substantially, ie 3, 4, 5, 6, 7, 8, 9 or 10 bar above the pressure level of the pressure column and thus the highest pressure level used in the column system.
  • the pressure difference can be up to 14, 16, 18 or 20 bar, for example.
  • turbo compressors In air separation plants, multi-stage turbo compressors are used to compress all of the separated air, which are referred to here as “main air compressors” or “main compressors” for short.
  • the mechanical structure of turbo compressors is known in principle to those skilled in the art.
  • a turbo compressor the medium to be compressed is compressed by means of turbine blades or impellers, which are arranged on a turbine wheel or directly on a shaft.
  • a turbo compressor forms a structural unit which, however, can have several compressor stages in the case of a multi-stage turbo compressor.
  • a compressor stage generally includes a turbine wheel or a corresponding arrangement of turbine blades. All of these airends can be driven by a common shaft. However, it can also be provided that the compressor stages are driven in groups with different shafts, in which case the shafts can also be connected to one another via gears.
  • the main air compressor is distinguished by the fact that it compresses the entire amount of air fed into the column system and used and broken down for the production of air products, i.e. the entire feed air.
  • a "post-compressor" can also be provided, in which, however, only part of the air quantity compressed in the main air compressor is brought to an even higher pressure.
  • This can also be designed as a turbo compressor.
  • Additional turbo compressors are typically provided for compressing partial amounts of air, which are also referred to as boosters, but only perform compression to a relatively small extent in comparison to the main air compressor or the secondary compressor.
  • a booster can also be present in a high-air pressure process, however, this then compresses a subset of the air starting from a correspondingly higher pressure level.
  • Air can also be expanded at several points in air separation plants, for which purpose, among other things, expansion machines in the form of turboexpanders, also referred to here as “expansion turbines”, can be used.
  • Turboexpanders can also be coupled to and drive turbocompressors. If one or more turbo compressors are driven without externally supplied energy, i.e. only via one or more turbo expanders, the term “turbine booster” or “booster turbine” is also used for such an arrangement.
  • the turboexpander (the expansion turbine) and the turbocompressor (the booster) are mechanically coupled, with the coupling being able to take place at the same speed (e.g. via a common shaft) or at different speeds (e.g. via an intermediate gear).
  • Liquid, gaseous or fluids in the supercritical state can be rich or poor in one or more components in the language used here, with “rich” for a content of at least 75%, 90%, 95%, 99%, 99.5% , 99.9% or 99.99% and “poor” can stand for a 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” just given, but in particular denotes a content of more than 90%. If, for example, "nitrogen” is mentioned here, it can be a clean gas, but it can also be a gas rich in nitrogen.
  • pressure level and “temperature level” are used below to characterize pressures and temperatures, which is intended to express the fact that pressures and temperatures do not have to be used in the form of exact pressure or temperature values in order to implement an inventive concept. However, such pressures and temperatures typically range within certain ranges, for example ⁇ 1%, 5% or 10% around an average value. Different pressure levels and temperature levels can be in disjunctive areas or in areas that overlap. In particular, for example, pressure levels include unavoidable or to be expected pressure losses, for example due to cooling effects. The same applies to temperature levels.
  • the pressure levels given here in bar are absolute pressures, unless otherwise stated.
  • HAP process is typically more cost-efficient than conventional MAC-BAC processes in terms of production costs and some operating costs due to the small number of rotating machines and the higher pressures that occur, there are usually disadvantages in terms of energy consumption.
  • the present invention is based on the finding that a modification of a corresponding "excess air" process offers particular advantages.
  • part of the overall compressed and cooled air is turbine-expanded, but not (as in a Joule-Thomson turbine) fed into the pressure column or (as in a Lachmann turbine) fed into the low-pressure column and separated there , but heated again to a temperature level on the warm side of the same in the main heat exchanger without being broken down and discharged from the system.
  • the relaxation can be particular atmospheric pressure.
  • air can be compressed (HAP) in the main air compressor to a high pressure, e.g.
  • HAP high pressure
  • the air can then be further compressed in one or two boosters, usually connected in series.
  • the boosters are driven by turbines.
  • a turbine expands the pressure above the HAP pressure achieved by means of the booster to the pressure column pressure (e.g. 5.6 bar).
  • This air is then divided into the necessary pressure column air (which is required for rectification) and an excess portion.
  • the excess portion (the "excess air”, also referred to as excess air in the following) is heated in the main heat exchanger and fed to a second turbine, which drives the second booster or (depending on the liquid performance in relation to the internal compression quantity) a generator and relaxes it to a pressure that is slightly is above ambient pressure. This portion is then heated in the main heat exchanger and e.g. blown off into the environment.
  • the present invention enables an improvement in the performance (in terms of the total cost of ownership, TCO) of HAP processes, especially in the case under consideration with a high liquid production, in which the use of an excess air turbine makes sense.
  • the present invention can be used in particular in cases in which more than 35%, in particular more than 40% or more than 50% of liquid air products, based on the amount of internally compressed air products, are removed from the air separation plant at least at times.
  • the present invention makes use of the fact that the so-called injection equivalent is not fully utilized in many systems and operating cases. It is known that increasing the injection equivalent can improve energy absorption.
  • the term blown-in air quantity refers to the compressed air expanded with a typical Lachmann turbine ("blow-in turbine") and fed (“blown-in”) into the low-pressure column.
  • the air expanded in this way into the low-pressure column disturbs the rectification, which is why the amount of air that can be expanded in the injection turbine and thus the cold that can be generated in this way for a corresponding system are limited.
  • Nitrogen-rich air products which are removed from the pressure column and carried out from the air separation plant, also influence the rectification in this way.
  • the amount of air injected into the low pressure column plus the nitrogen removed from the pressure column and discharged from the air separation plant can be stated in relation to the total air fed into the column system. The value obtained is the "blow-in equivalent".
  • the injection equivalent is therefore defined as the amount of compressed air that is compressed and expanded by means of an injection turbine into the low-pressure column of an air separation plant plus the amount of nitrogen that may have been removed from the pressure column and not returned to the pressure column itself as liquid reflux or to the low-pressure column as liquid reflux is given up, based on the total compressed air fed into the column system.
  • the nitrogen that is taken from the pressure column can be pure or essentially pure nitrogen from the top of the pressure column, but also a nitrogen-enriched gas that can be drawn off with a lower nitrogen content from an area below the top of the high-pressure column.
  • the present invention proposes a process for obtaining one or more air products, in which an air separation plant is used which has a column system with a pressure column, the pressure column being in a pressure range of 4 to 7 bar, for example 5 to 6 bar, in particular approx 5.6 bar, with air being supplied to the column system and being separated in the column system, and with at least 90% of the total air supplied to the column system, in particular more than 95% or all of the air, being compressed to a base pressure level which is more than 5 bar above the pressure range at which the pressure column is operated, for example at 20 to 30 bar, in particular about 23 bar.
  • a HAP method is used.
  • Nitrogen-rich gas is removed from the pressure column and, at least in a first operating mode, further air is compressed to a pressure level above the base pressure level, expanded and heated in the column system without decomposition.
  • part of the nitrogen-rich gas taken from the pressure column is fed to the further air upstream of the expansion.
  • the feeding can take place before the further air is heated, in which case the further air and the supplied nitrogen-rich gas are heated together, in particular in the main heat exchanger.
  • it can also be fed in after the additional air has been heated, in which case the additional air and the nitrogen-rich gas fed in are then previously heated separately from one another, in particular in the main heat exchanger. Both alternatives are explained in more detail below as embodiments of the invention.
  • the injection equivalent By feeding the nitrogen-rich gas taken from the pressure column to the excess air, the injection equivalent can be better utilized. This feed (in an amount that depends on the product constellation and the correspondingly optimal injection equivalent) reduces the excess air that is required. The power of the turbine used to expand the excess air remains about the same because the additional amount of the The nitrogen-rich gas extracted from the pressure column compensates for the reduction in excess air.
  • the injection equivalent since the injection equivalent is increased, the amount of air for rectification increases. Overall, however, the amount of air required at the main air compressor is reduced. Depending on the product constellation, the reduction can be up to approx. 6%. The reduction translates directly into energy savings. However, increasing the blowing equivalent also decreases the argon yield, but reduces the overall cost.
  • the present invention can be implemented in different modes of operation, whereby the aforementioned "first" mode of operation can also be the only mode of operation.
  • a second operating mode can be provided, in which case the additional air is also compressed to a pressure level above the base pressure level in the second operating mode, expanded and heated in the column system without decomposition (i.e. excess air is used), and in the second operating mode no nitrogen-rich gas taken from the pressure column is fed to the further air.
  • the injection equivalent can be lowered temporarily in the second operating mode, for example, if increased argon production is desired.
  • a third operating mode can also be provided.
  • the numbering is only done here for the sake of clarification; there does not have to be a second operating mode and the method can also include, for example, only the first and third operating modes.
  • no further air is compressed to a pressure level above the base pressure level, expanded and without decomposition in the column system (that is to say no excess air is used), and in the third operating mode part of the nitrogen-rich gas removed from the pressure column is expanded and heated instead of the additional air.
  • the injection equivalent can be correspondingly increased in the third operating mode.
  • the additional air can be fed successively on the warm side to a main heat exchanger of the air separation plant for use as excess air at the pressure level above the base pressure level, removed from the main heat exchanger at a first intermediate temperature level, subjected to a first turbine expansion, fed to the main heat exchanger on the cold side, fed to the main heat exchanger on a removed from the second intermediate temperature level, subjected to a second turbine expansion, fed to the main heat exchanger at a third intermediate temperature level, and removed from the hot side of the main heat exchanger.
  • the part of the nitrogen-rich gas taken from the pressure column, which is fed to the further air, i.e. the excess air, can in particular be fed to the main heat exchanger together with the further air on the cold side after its first turbine expansion, subjected to the second turbine expansion, fed to the main heat exchanger at the third intermediate temperature level, and the main heat exchanger are taken from the warm side.
  • the nitrogen-rich gas is heated here together with the other air.
  • the part of the nitrogen-rich gas taken from the pressure column, which is fed to the further air, i.e. the excess air, but also fed to the main heat exchanger on the cold side can be taken off on the hot side and fed to the further air at the second intermediate temperature level and before the second turbine expansion . In this configuration, therefore, separate heating takes place.
  • the base pressure level (HAP pressure) within the scope of the present invention can be 11 to 28 bar, in particular 16 to 24 bar, for example approximately 23 bar.
  • the pressure level above the base pressure level to which the additional air, i.e. the air used to provide the excess air, is compressed can be increased in each subsequent booster by a factor of 1.1 to 1.6, in particular by a factor of 22 to 50 bar, for example 22 to 30 bar in Systems where the second turbine expansion of the excess air is performed in a turbine coupled to a generator and 35 to 50 bar in systems where the second turbine expansion of the excess air is performed in a turbine coupled to a booster.
  • the pressure range in which the pressure column is operated can be, in particular, 4 to 7 bar, for example 5 to 6 bar, in particular about 5.6 bar, as mentioned.
  • the main heat exchanger can be operated at a temperature level of 0 to 50 °C on the warm side and at a temperature level of -150 to -177 °C on the cold side.
  • the mentioned first intermediate temperature level can be -120 to -90 °C
  • the second intermediate temperature level can be -20 to 30 °C
  • the third intermediate temperature level can be -110 to -60 °C.
  • the first turbine expansion can be carried out at a pressure level of 4 to 7 bar and the second turbine expansion can be carried out at a pressure level of 100 mbar to 500 mbar above atmospheric pressure.
  • the additional air i.e. the air used to provide the excess air
  • the additional air can be compressed to the pressure level above the base pressure level using one or two boosters, with one booster or at least one of the two boosters using at least one of the expansion machines is or are driven, which are used in the mentioned first and second turbine relaxation.
  • a booster it can be driven using the expander used in the first or second turbine expansion, or when using two boosters, one of them can be driven using the expander used in the first turbine expansion and the other of them can be driven using the be driven in the second turbine expansion used expansion machine.
  • the respective assignment is arbitrary.
  • one of the expansion machines can also be braked, for example by means of a generator or in some other way, in which case the further air is typically only compressed to the pressure level above the base pressure level using a booster.
  • the other air that is compressed to the pressure level above the base pressure level, expanded and heated without decomposition in the column system i.e. the air used as excess air
  • This air, which is fed into the column system and which is compressed together with the other air to the pressure level above the base pressure level can in particular be cooled to a first proportion and fed into the column system without being subjected to the first and second expansion, and a second portion in liquefied form are separated after the first expansion and fed into the column system.
  • the present invention also extends to an air separation plant.
  • an air separation plant For features and advantages of such an air separation plant, reference is made to the corresponding independent patent claim.
  • such an air separation plant is set up to carry out a method in one or more of the configurations explained above and has appropriately designed means for this purpose.
  • FIG. 1 shows an air separation plant not designed according to the invention in a simplified representation.
  • FIG. 2 shows an air separation plant designed according to an embodiment of the invention in a simplified representation.
  • FIG. 3 shows an air separation plant configured according to an embodiment of the invention in a simplified representation.
  • FIG. 1 shows an air separation plant not designed according to the invention in the form of a simplified process flow diagram.
  • air is sucked in from the atmosphere A by means of a main air compressor 1 via a filter 2 and compressed to the base pressure level mentioned several times above.
  • a compressed air flow a provided in this way is fed to an adsorber station 3 after cooling in heat exchangers (not designated separately) and separation of water W, where it is freed from undesirable components such as water and carbon dioxide.
  • the compressed air flow a is divided into two partial flows b and c.
  • Partial flow b is fed to a main heat exchanger 4 at the warm end and removed at the cold end.
  • the partial flow c is further compressed using two boosters 5 and 6 and then also fed to the main heat exchanger 4 at the warm end. Again a partial flow d of the partial flow c is taken from the main heat exchanger 4 at the cold end.
  • the partial streams b and d are throttle-expanded, liquefied at least in part, combined and fed into a pressure column 11 of a column system 10 in the form of a material stream that is not designated separately.
  • the column system 10 has a low-pressure column 12 connected to the pressure column 11 in the form of a double column and thermally coupled via a main condenser 13 .
  • a supercooling countercurrent 14 and an argon recovery part 15 of conventional design are provided, by means of which pure argon X can be recovered. The latter can be operated as often described in the technical literature.
  • a low-temperature rectification is carried out at a rectification pressure level.
  • Another partial flow e of the partial flow c is taken from the main heat exchanger 4 at an intermediate temperature level, expanded in an expansion turbine 7 coupled to the booster 5, thereby partially liquefied, and fed into a separator 9, where a liquid phase and a gas phase form.
  • the liquid phase is conducted in the form of a stream f through the subcooling countercurrent 14 and then fed into the low-pressure column 12 .
  • the gas phase is divided into two partial streams g and h.
  • Partial stream g is fed into pressure column 11 .
  • the partial stream h is fed to the main heat exchanger 4 at the cold end and removed from it near the warm end. It is then expanded in an expansion turbine 8 coupled to the booster 6, fed back to the main heat exchanger 4 at an intermediate temperature level, removed from this at the warm end, and discharged from the plant. This is the so-called excess air, also denoted by H here. Since the partial flow h already includes cleaned air, it can, for example, be compressed again in the main air compressor 2 and used to form the compressed air flow a in order to reduce the cleaning effort.
  • a nitrogen-rich top gas is formed at the top of the pressure column 11, part of which is heated in gaseous form in the form of a stream i in the main heat exchanger 4 and discharged as a pressure product I from the air separation plant. Another part is at least partially condensed in the main condenser 13 . A first part (unmarked) of the condensate formed is fed back to the pressure column 11 as reflux, a second part is provided in the form of a stream k as internally compressed nitrogen product K and a third part in the form of a stream m through out the supercooling countercurrent 14 and fed into the low-pressure column 12 as reflux at its head.
  • the low-pressure column 12 is mainly fed with bottom liquid from the pressure column 11, which is removed from it in the form of a stream o.
  • the bottom liquid from the pressure column 11 is used to cool overhead condensers in the argon recovery section 15 and is partially evaporated there. Evaporated and non-evaporated fractions are transferred to the low-pressure column 12, as illustrated here in the form of the streams p.
  • the argon recovery section 15 is materially connected to the low-pressure column 12 via material flows q, which are not explained in detail here. Liquid air is also fed into the low-pressure column 12 in the form of a stream n, which is taken from the pressure column 11 directly below the feed point for the streams b and d and passed through the supercooling countercurrent 14 .
  • Bottom liquid from the low-pressure column 12 can be removed from it in the form of a stream r and provided in part in the form of a stream s as liquid nitrogen S and in part in the form of a stream t to provide internal compression products T1, T1.
  • Gaseous nitrogen can be drawn off from the top of the low-pressure column 12 in the form of a stream u, and liquid nitrogen can be drawn off in the form of a stream v.
  • the latter can be provided as liquid nitrogen V, as well as a partial flow of material flow m as pressurized liquid nitrogen M.
  • FIG. 2 shows an air separation plant designed according to an embodiment of the invention in a simplified representation. This is denoted overall by 100 and includes all of the components of the air separation plant illustrated in FIG.
  • FIG. 3 shows an air separation plant designed according to a further embodiment of the invention in a simplified representation. This is denoted overall by 200 and includes all of the components of the air separation plant 100 illustrated in FIG. The partial flow c is thus compressed only by means of the booster 5.
  • FIG. 4 shows an air separation plant designed according to a further embodiment of the invention in a simplified representation. This is denoted overall by 300 and includes all the components of the air separation plant 100 illustrated in Figure 2, but in contrast to that, instead of the local material flow w, a material flow x is branched off from the material flow i on the hot side of the main heat exchanger 4 and fed to the material flow h.

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  • 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

L'invention concerne un procédé d'obtention d'un ou de plusieurs produits à base d'air. Dans ledit procédé, une installation de fractionnement d'air est utilisée et comporte un système de colonnes (10) avec une colonne de pression (11), la colonne de pression (11) étant actionnée dans une plage de pression de 4 à 7 bar, l'air étant introduit dans le système de colonne (10) et étant fractionné dans le système de colonne (10), au moins 90 % de la quantité totale d'air fournie au système de colonne (10) étant comprimée à un niveau de pression de base qui est supérieur à 5 bar au-dessus de la plage de pressions à laquelle fonctionne la colonne de pression (11), le gaz riche en azote étant extrait de la colonne de pression (11), et, au moins dans un premier mode de fonctionnement, l'air supplémentaire qui est comprimé jusqu'à un niveau de pression au-dessus du niveau de pression de base, étant expansé, et étant chauffé sans fractionnement dans le système de colonne (10). Il est prévu que, au moins dans le premier mode de fonctionnement, une proportion du gaz riche en azote extrait de la colonne de pression (11) est introduite dans l'air supplémentaire en amont de l'expansion. La présente invention concerne également une installation de fractionnement d'air correspondante.
EP21751977.6A 2020-09-08 2021-07-28 Procédé d'obtention d'un ou de plusieurs produits à base d'air, et installation de fractionnement d'air Pending EP4211409A1 (fr)

Applications Claiming Priority (2)

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EP20020403 2020-09-08
PCT/EP2021/025287 WO2022053172A1 (fr) 2020-09-08 2021-07-28 Procédé d'obtention d'un ou de plusieurs produits à base d'air, et installation de fractionnement d'air

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US (1) US20230358466A1 (fr)
EP (1) EP4211409A1 (fr)
CN (1) CN116018491A (fr)
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WO (1) WO2022053172A1 (fr)

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Publication number Priority date Publication date Assignee Title
GB727911A (en) * 1952-07-28 1955-04-13 Nat Res Dev Improvements in or relating to the separation of one or more constituents of a gaseous mixture
JPS5146073B1 (fr) 1969-08-12 1976-12-07
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2980514A1 (fr) 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air
DE102016015446A1 (de) * 2016-12-23 2018-06-28 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage
EP3343158A1 (fr) 2016-12-28 2018-07-04 Linde Aktiengesellschaft Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air
CN211926303U (zh) * 2020-03-11 2020-11-13 苏州市兴鲁空分设备科技发展有限公司 全液体空分设备

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CN116018491A (zh) 2023-04-25

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