WO2023030689A1 - Procédé pour obtenir un ou plusieurs produits de l'air et installation de séparation d'air - Google Patents

Procédé pour obtenir un ou plusieurs produits de l'air et installation de séparation d'air Download PDF

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Publication number
WO2023030689A1
WO2023030689A1 PCT/EP2022/025401 EP2022025401W WO2023030689A1 WO 2023030689 A1 WO2023030689 A1 WO 2023030689A1 EP 2022025401 W EP2022025401 W EP 2022025401W WO 2023030689 A1 WO2023030689 A1 WO 2023030689A1
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WIPO (PCT)
Prior art keywords
air
pressure
heat exchanger
air flow
flow
Prior art date
Application number
PCT/EP2022/025401
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German (de)
English (en)
Inventor
Daniel OTTE
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Linde Gmbh
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Publication date
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Publication of WO2023030689A1 publication Critical patent/WO2023030689A1/fr

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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
    • F25J3/04642—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
    • F25J3/04006—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
    • F25J3/04151—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
    • F25J3/04151—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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure 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
    • F25J3/04284—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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
    • F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
    • 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
    • F25J3/04721—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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

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/recompressor processes are characterized in that only part of the total amount of feed air fed to the column system is compressed to a pressure level that is significantly, i.e. by 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 fed into the pressure column at this 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 gearbox).
  • 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” or “pressure range” and “temperature range” are used to characterize pressures and temperatures, which is intended to express that pressures and temperatures are not used in the form of exact pressure or temperature values must in order to realize an inventive concept.
  • 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.
  • pressure levels include unavoidable or to be expected pressure losses, for example due to cooling effects.
  • the pressure levels given here in bar are absolute pressures, unless otherwise stated.
  • a "main heat exchanger" of an air separation plant is a heat transfer apparatus in which typically all or the majority of the air to be separated in the air separation plant is cooled, in particular in countercurrent to at least a major part or all of the gaseous air provided by the air separation plant air products.
  • the main heat exchanger can have one or more identically or differently constructed heat exchanger blocks of a known type, which in particular can be operated in parallel.
  • the heat exchangers or heat exchanger blocks used in the invention are in particular designed as brazed fin-plate heat exchangers made of aluminum (Brazed Aluminum Plate-Fin Heat Exchangers, PFHE; designations according to the German and English editions of ISO 15547-2:3005), as they be used in a large number of process engineering systems at different pressures and temperatures.
  • Brazed aluminum plate-fin heat exchangers are shown in Figure 2 of ISO 15547-2:3005 and on page 5 of ALPEMA publication "The Standards of the Brazed Aluminum Plate-Fin Heat Exchanger Manufacturers' Association", 3rd edition 2010 and described.
  • heat exchanger block stands here in particular for a unit produced by (vacuum) brazing, which consists of structural plates, distributor lamellae, so-called Sidebars, dividers and cover plates is formed and are applied to the so-called header.
  • a corresponding rib-plate heat exchanger can be formed from a plurality of corresponding cuboid heat exchanger blocks connected to one another, in particular for manufacturing reasons.
  • HAP processes are 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 (in a so-called excess air turbine, but not (as in a Joule-Thomson turbine) into the pressure column or (as in a Lachmann turbine) fed into the low-pressure column and broken down 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 expansion can take place in particular to atmospheric pressure.
  • air can be compressed in the main air compressor to a high pressure, for example 23 bar (high air pressure method).
  • the air can then be further compressed in two boosters connected in series.
  • the boosters are driven by turbines.
  • a turbine expands the pressure achieved by means of the booster above the already high outlet pressure of the main air compressor 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 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 heat exchanger volume is greatly increased as the amount of excess air increases.
  • the reason is that the air expanded in the excess air turbine (at a pressure in a slightly superatmospheric pressure range of, for example, approx. 1.2 bar) enters the main heat exchanger at an inlet temperature of approx. 180 K and is heated to ambient temperature.
  • the cold part of the passages of the main heat exchanger required for this air (below the specified inlet temperature) cannot be used and is therefore empty volume. This makes up, for example, about 3/4 of the corresponding passages and thus about 10% of the total heat exchanger volume. In larger systems, this leads to a very large heat exchangers and thus high costs.
  • the present invention overcomes this disadvantage.
  • the present invention can be used in particular with large main heat exchanger volumes where, due to the size, several (at least two) heat exchanger blocks have to be used, for example with volumes of 30 to 100 m 3 or more, in particular 80 to 90 m 3 .
  • the empty volumes mentioned are disadvantageous, since this occurs in all heat exchanger blocks.
  • the invention creates a solution here that reduces the investment costs (CAPEX) without causing disadvantages in the operating costs (OPEX).
  • the present invention solves this problem in that the heating of the excess air is detached from the main heat exchanger and is carried out in a separate counterflow heat exchanger. At least one warm stream must be conducted in countercurrent, as explained further below with regard to specific configurations of the invention.
  • a "separate" counterflow heat exchanger whose heat exchanger block(s) is/are provided separately from the heat exchanger block or the heat exchanger blocks of the main heat exchanger, with the heat exchanger blocks only being connected via lines and, if necessary, fastening structures, but these heat exchangers, each designed in particular as a rib-plate heat exchanger, in particular have no common heat exchanger plates.
  • the present invention proposes a method for obtaining one or more air products, in which an air separation plant is used which has a column system with a pressure column and a low-pressure column and a main heat exchanger, the pressure column being in a first pressure range of in particular 4 to 7 bar, for example 5 to 6 bar, in particular at approx. 5.6 bar, and the low-pressure column is operated in a second pressure range of in particular 1 to 2 bar, in particular for example at 1.2 bar to 1.5 bar, in particular at approx. 1.4 bar, is operated.
  • Air is supplied to the column system which is broken down in the column system, and the amount of which is referred to here as the break-up air amount.
  • an initial quantity of air which in particular completely encompasses the quantity of separation air, is compressed to a pressure in a third pressure range which is at least 5, 10, 15 or 20 bar above the first pressure range, for example a third pressure range of 20 to 50 bar, in particular about 25 to 40 bar.
  • the third pressure range can also include pressures which are 1.1 to 1.9 times, in particular 1.3 to 1.6 times, the pressures in the first pressure range.
  • a proportion of at least 90% of the total amount of separation air separated in the column system, in particular more than 95% thereof or the entire amount of separation air, is formed by a first partial amount of the initial air amount, which is compressed to the pressure in the third pressure range.
  • a HAP method is therefore used within the scope of the invention.
  • air from the initial air quantity is subjected to stepwise sequential compression from the pressure in the third pressure range (via a pressure in an intermediate pressure range) to a pressure in a fourth pressure range, which is above the third pressure range, to obtain a high-pressure air stream, with below Using air from this high-pressure air flow, a compressed air flow, hereinafter referred to as "follow-up air flow", is formed, which is discharged from the main heat exchanger at a pressure in the fourth pressure range and at an intermediate temperature in a temperature range of 130 to 190 K.
  • the intermediate temperature can be 135 to 145 K, in particular approx 145 K, in particular approx. 144 K.
  • the invention is not limited to these specific configurations and is also not defined accordingly in the respective explained embodiments, ie the temperatures can also be in the other respective ranges or in between.
  • the product constellation internal compression pressure
  • different variants can be advantageous.
  • the entire high-pressure air flow does not have to be used to form the subsequent air flow, whereas in other embodiments this is the case.
  • Additional air from the initial air quantity can also be passed through the main heat exchanger, for example as a throttle flow without further compression, i.e. at the pressure in the third pressure level, and without further pressure-influencing measures such as compression and expansion, then in particular liquefied, and then into the column system, in particular the pressure column , be relaxed.
  • the aforementioned subsequent compression to form the high-pressure air flow is carried out in the context of the present invention using a first booster and using a second booster, i.e. serially via an intermediate pressure and in particular using after-cooling, in particular with water, downstream of each of the boosters, where the first and second booster and the first and second turbine are each mechanically coupled to one another in any way, in particular in pairs.
  • the first booster can be driven using the first or second turbine and the second booster can be driven using the other turbine.
  • air of the subsequent air flow is subjected to expansion in the first turbine, to which the subsequent air flow is supplied at the temperature in the mentioned temperature range at which it is taken from the main heat exchanger, and thereafter, i.e. after expansion in the first Turbine used to form a separation air stream, wherein air of the separation air stream is separated in the column system.
  • a first operating mode which can also be the only operating mode
  • further air of the subsequent air flow is subjected to expansion in the first turbine and then used to form an excess air flow, the air of which is expanded and heated without prior separation in the column system.
  • the In the first operating mode correspondingly treated air from the excess air stream is successively subjected to heating in the main heat exchanger, expansion in the second turbine (in particular to ambient pressure or a slightly above-atmospheric pressure in the second pressure range) and further heating (in particular to approximately ambient temperature). .
  • the further heating of the air of the excess air stream in the first operating mode is carried out using a further heat exchanger which has a heat exchanger block which is provided separately from a heat exchanger block of the main heat exchanger, and that in the further heat exchanger air of the initial air quantity in the first mode of operation is subjected to cooling.
  • a further heat exchanger which has a heat exchanger block which is provided separately from a heat exchanger block of the main heat exchanger, and that in the further heat exchanger air of the initial air quantity in the first mode of operation is subjected to cooling.
  • the first operating mode can be the only operating mode or a second operating mode can be provided in addition to the first operating mode, in which the excess air flow is not formed and in particular the further heat exchanger cannot be in operation. This can be provided in particular in cases in which a (comparatively) low level of liquid production is to take place.
  • a partial flow of the excess air to be heated can be mixed with an impure nitrogen flow from the low-pressure column after expansion in the second turbine and heated in the main heat exchanger.
  • the air subjected to cooling in the further heat exchanger is then subjected in the main heat exchanger to a combination with a further proportion of the air of the high-pressure air flow, which is fed to the main heat exchanger on the warm side, in order to form the subsequent air flow.
  • the subsequent air flow is thus formed here using two portions of the high-pressure air flow, one of which is cooled in the main heat exchanger without further pressure-influencing measures, but the other is cooled in the separate heat exchanger. Both parts are combined at a suitable intermediate temperature level in the main heat exchanger, cooled further in this and removed from it in the form of the subsequent air flow.
  • the proposed measure has the advantage that the passages relocated to the additional heat exchanger do not have to be provided in the main heat exchanger, where they would lead to unused space on the cold side of the extraction of the subsequent air flow. With certain product constellations, however, the two portions can also be routed separately through the main heat exchanger without being combined at the intermediate temperature level. This is therefore not absolutely necessary
  • At least 90% of an amount of air resulting from the combination in particular 95% of this amount of air or the entire amount of air, is used to form the subsequent air flow.
  • the air subjected to the cooling in the further heat exchanger is a portion of the air of the output air quantity at a pressure in the third pressure range which is not used to form the high-pressure air flow.
  • the main heat exchanger to form a Joule-Thomson flow in a manner known per se, is subjected to a combination with further air, not used to form the high-pressure air flow, of the initial air quantity.
  • the Joule-Thomson flow formed in this way can be further cooled, particularly in the main heat exchanger.
  • this Joule-Thomson current can also be provided in addition to any other current, for example an above-mentioned Joule-Thomson current.
  • At least 90% of an amount of air resulting from the combination can be used to form the Joule-Thomson current.
  • a first proportion of the air of the high-pressure air stream can also be used to form the follow-on stream and a second proportion of the air of the high-pressure air stream can be further cooled in the main heat exchanger and combined with the Joule-Thomson stream on the cold side thereof.
  • the air subjected to cooling in the further heat exchanger can be cooled to a temperature in a suitable temperature range, this temperature range depending in particular on the temperature range in which the second turbine is operated.
  • This temperature range can in particular be 2 to 15 K or 20 K above the outlet temperature of the second turbine.
  • the temperature range can be in particular 190 to 195 K, and in the second group of configurations in particular 195 to 200 K, in particular about 196 K.
  • the excess air flow can be supplied to the further heat exchanger, in particular at a temperature in a temperature range from 165 to 210 K, in particular at approx. 184 K, which temperature is achieved by the expansion in the second turbine, and this excess air flow can be formed in particular as a single-phase (gaseous) flow as a result of the expansion in the second turbine.
  • the air of the excess air stream before being expanded in the second turbine can start from a temperature in a temperature range of 90 to 115 K and to a temperature in a temperature range from 240 K to ambient temperature, a temperature in a temperature range from 270 to 290 K being particularly advantageous. This corresponds to the outlet temperature of the cold turbine.
  • one or more air products are provided by means of internal compression, wherein more than 35% of liquid air products, based on the (entire) quantity of internally compressed air products, are provided at least at times.
  • this also includes the exclusive provision of liquid air products without the provision of internally compressed air products.
  • 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 configured according to one embodiment of the invention in a simplified representation.
  • FIG. 3 shows an air separation plant designed according to an embodiment of the invention in a simplified partial representation.
  • the same or comparable elements are given identical reference numbers and are not explained again for the sake of clarity.
  • Components illustrated identically in several figures are in part not provided with reference symbols again.
  • Plant components can each also stand for corresponding process steps, so that the following explanations on the air separation plants also relate to corresponding processes.
  • FIG. 1 an air separation plant according to one embodiment of the invention is illustrated in the form of a simplified process flow diagram and is labeled 100 overall.
  • air is sucked in from the atmosphere by means of a main air compressor 1 via a filter that is not designated separately and is compressed to the pressure in the third pressure range that has been mentioned several times before. This is the output air volume, which has been mentioned several times.
  • a compressed air stream A provided in this way is fed to an adsorber station 2 after cooling in heat exchangers (not designated separately) and separation of water, where it is freed from undesirable components such as water and carbon dioxide.
  • the compressed air flow A i.e. the output air volume, is divided into two partial flows B and C.
  • Partial flow B is conducted as a Joule-Thomson flow from the warm to the cold end through a main heat exchanger 3, where it is at least partially liquefied and then fed into a pressure column 11 of a column system 10, which is operated in the first pressure range mentioned several times. Liquid is withdrawn immediately below the feed point of partial stream B into the pressure column 11, which is conducted through a supercooling countercurrent flow device 14 and fed into a low-pressure column 12 of the column system 10 operated in the second pressure range mentioned several times.
  • the column system 10 which also has an argon recovery part designated as a whole by 13, is operated in a manner customary in the art.
  • the partial flow C i.e. also air of the initial air quantity
  • the partial flow C is subjected to a gradual sequential compression from the pressure in the third pressure range to a pressure in a fourth pressure range, which is above the third pressure range, to obtain a high-pressure air flow D, using air from the high-pressure air flow D, as explained further below, a follow-up air flow E is formed, which is discharged from the main heat exchanger at a pressure in the fourth pressure range and at an intermediate temperature in the mentioned range.
  • the subsequent compression of the partial flow C to form the high-pressure air flow D takes place in the specific example in succession using a first booster 4, which is driven using a first turbine 5, and using a second booster 6, which is driven using a second turbine 7 .
  • Air of the follow-up air flow E is subjected to expansion in the first turbine 5 and then, according to the configuration according to FIG.
  • an excess air flow Y is drawn off immediately above the feed of the material flow X into the pressure column 11, which is fed to the main heat exchanger 3 on the cold side and removed at an intermediate temperature level, then expanded in the second turbine 7, from the cold side to the warm side by a further one Heat exchanger 8 out and discharged, for example, to the atmosphere or otherwise used.
  • the air separation plant differs from an air separation plant not designed according to the invention in particular in that a further heat exchanger 8 is provided.
  • air from the subsequent air flow E is subjected to expansion in the first turbine 5 and then fed into the pressure column 11 in the form of a material flow X.
  • An excess air flow is formed with the substance flow Y, whereas the remainder is separated as a separation air flow in the column system 10 .
  • the (further) heating of the air of the stream Y is thus carried out using the further heat exchanger 8, which has a heat exchanger block that is provided separately from a heat exchanger block of the main heat exchanger 3, wherein in the further heat exchanger 8 air of the initial air quantity, here a partial flow D1 of the high-pressure air stream D, is subjected to cooling.
  • the configuration according to FIG. 1 thus belongs to the first group of configurations mentioned several times, in which the air subjected to cooling in the additional heat exchanger 8 is a proportion of the air of the high-pressure air flow, designated here as D1.
  • the air of the material flow D1 subjected to cooling in the further heat exchanger 8 is then subjected to a combination in the main heat exchanger 3 to form the follow-on air flow E with a further portion of the air of the high-pressure air flow, denoted here by D2, and which is fed to the main heat exchanger 3 on the warm side becomes.
  • a collecting flow formed in this way is carried out as the follow-up air flow E from the main heat exchanger 3 .
  • the union is not mandatory.
  • FIG. 2 shows an air separation plant designed according to an embodiment of the invention in a simplified partial representation, which corresponds in parts to FIG. The integration results from the identical designation of the respective plant parts and material flows.
  • the air in the follow-on air flow E is used here after expansion in the first turbine 5 and before it is still upstream of the pressure column 11 to form a separation air flow F and an excess air flow G, with the excess air flow G being essentially the same as in Figure 1 explained can be treated.
  • the configuration according to FIG. 2 also belongs to the first group of configurations, in which the air subjected to cooling in the further heat exchanger 8 is a portion of the air of the high-pressure air stream, designated D1 here.
  • the air of the material flow D1 subjected to cooling in the further heat exchanger 8 is then combined in the main heat exchanger 3 to form the subsequent air flow E with a further proportion of the air of the high-pressure air flow, which is designated here as D2, and which is fed to the main heat exchanger 3 on the hot side becomes.
  • a collecting flow formed in this way is carried out as the follow-up air flow E from the main heat exchanger 3 .
  • FIG. 3 shows an air separation plant designed according to an embodiment of the invention in a simplified partial representation, which corresponds in parts to the previously explained embodiments, with a corresponding plant being denoted by 100 .
  • the air of the subsequent air flow E according to Figure 3 is used after expansion in the first turbine 5 and before it is still upstream of the pressure column 11 to form a separation air flow F and an excess air flow G, with the excess air flow G essentially can be treated as explained with reference to FIGS.
  • a Joule-Thomson current is formed using another part of the material flow D.
  • the air of the material flow G1 which has been subjected to cooling in the further heat exchanger 8, is then combined in the main heat exchanger 3 to form a Joule-Thomson flow H1 with a further proportion of the air in the initial air quantity at a pressure in the third pressure range, which does not lead to the Formation of the high-pressure air stream is used, and which is illustrated here in the form of a stream G2.
  • a material flow H1 formed in this way is removed from the main heat exchanger 3 at the cold end.

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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 l'obtention d'un ou de plusieurs produits de l'air au moyen d'un procédé de séparation de l'air sous haute pression d'air faisant appel une turbine à air excédentaire. De l'air d'une quantité d'air de sortie est soumis à une compression consécutive par paliers afin d'obtenir un flux d'air à haute pression, un flux d'air résultant étant formé à l'aide d'air du flux d'air à haute pression. La compression consécutive est effectuée succesivement à l'aide d'un premier surpresseur (4) qui est entraîné à l'aide d'une première turbine (5), et à l'aide d'un deuxième surpresseur (6) qui est entraîné à l'aide d'une deuxième turbine (7). De l'air du flux d'air résultant est soumis à une détente dans la première turbine (5) et est ensuite utilisé pour former un flux d'air de séparation et un flux d'air excédentaire. Un chauffage du flux d'air excédentaire est effectué après sa détente à l'aide d'un échangeur de chaleur (8) supplémentaire qui comprend un bloc d'échangeur de chaleur fourni séparément d'un bloc d'échangeur de chaleur de l'échangeur de chaleur principal (3), de l'air de la quantité d'air de départ étant soumis à un refroidissement dans l'échangeur de chaleur (8) supplémentaire, et au moins une partie de l'air refroidi dans l'échangeur de chaleur principal étant combinée à une autre partie du flux d'air haute pression, et y est rechauffée. L'invention concerne en outre une installation de séparation d'air (100, 200) correspondante.
PCT/EP2022/025401 2021-09-02 2022-08-31 Procédé pour obtenir un ou plusieurs produits de l'air et installation de séparation d'air WO2023030689A1 (fr)

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Citations (8)

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Publication number Priority date Publication date Assignee Title
US3905201A (en) 1969-08-12 1975-09-16 Union Carbide Corp Air separation with work expansion to high and low pressure rectification stages
FR2928446A1 (fr) * 2008-03-10 2009-09-11 Air Liquide Procede de modification d'un appareil de separation d'air par distillation cryogenique
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
EP3255366A1 (fr) * 2016-06-09 2017-12-13 Linde Aktiengesellschaft Procédé et dispositif de production d'un produit gazeux à base d'oxygène sous pression
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
EP3671085A1 (fr) * 2018-12-18 2020-06-24 Linde GmbH Dispositif et procédé de récupération de la chaleur de compression à partir de l'air comprimé et traité dans une installation de traitement de l'air

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Publication number Priority date Publication date Assignee Title
US3905201A (en) 1969-08-12 1975-09-16 Union Carbide Corp Air separation with work expansion to high and low pressure rectification stages
FR2928446A1 (fr) * 2008-03-10 2009-09-11 Air Liquide Procede de modification d'un appareil de separation d'air par distillation cryogenique
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
EP3255366A1 (fr) * 2016-06-09 2017-12-13 Linde Aktiengesellschaft Procédé et dispositif de production d'un produit gazeux à base d'oxygène sous pression
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
EP3671085A1 (fr) * 2018-12-18 2020-06-24 Linde GmbH Dispositif et procédé de récupération de la chaleur de compression à partir de l'air comprimé et traité dans une installation de traitement de l'air

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"Industrial Gases Processing", 2006, WILEY-VCH, article "Cryogenic Rectification"
F.G. KERRY: "Industrial Gas Handbook: Gas Separation and Purification", 2006, CRC PRESS, article "Contemporary Liquefaction Cycles"
W. DIERY: "The Manufacture of Plate-Fin Heat Exchangers at Linde", LINDE REPORTS ON SCIENCE AND TECHNOLOGY, vol. 37, 1984, pages 24 - 31

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