EP2600090B1 - Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air - Google Patents

Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air Download PDF

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Publication number
EP2600090B1
EP2600090B1 EP12007828.2A EP12007828A EP2600090B1 EP 2600090 B1 EP2600090 B1 EP 2600090B1 EP 12007828 A EP12007828 A EP 12007828A EP 2600090 B1 EP2600090 B1 EP 2600090B1
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Prior art keywords
air
pressure
substream
heat exchanger
compressed
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Not-in-force
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EP12007828.2A
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German (de)
English (en)
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EP2600090A1 (fr
Inventor
Alexander Alekseev
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—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
    • F25J3/04018—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 of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
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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
    • 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
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04096—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of argon or argon enriched stream
    • 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
    • F25J3/04248—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
    • F25J3/04333—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
    • 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
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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
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    • 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
    • F25J3/04703—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 being arranged in more than one vessel
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
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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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the invention relates to a method according to the preamble of patent claim 1.
  • the distillation column system of the invention may be designed as a two-column system (for example as a classic Linde double column system) or as a three-column or multi-column system. It may in addition to the columns for nitrogen-oxygen separation, further devices for obtaining high purity products and / or other air components, in particular of noble gases, for example, an argon production and / or a krypton-xenon recovery
  • a liquid pressurized oxygen product stream is vaporized against a heat carrier and finally recovered as a gaseous pressure product.
  • This method is also called internal compression. It serves for the production of pressure oxygen. In the case of a supercritical pressure, no phase transition takes place in the true sense, the product stream is then "pseudo-evaporated".
  • a high-pressure heat carrier is liquefied (or pseudo-liquefied when it is under supercritical pressure).
  • the heat transfer medium is often formed by part of the air, in the present case by the "second partial flow" of the compressed feed air.
  • EP 1139046 A1 EP 1146301 A1 .
  • DE 10213212 A1 DE 10213211 A1 .
  • EP 1357342 A1 or DE 10238282 A1 DE 10302389 A1 .
  • DE 10332863 A1 EP 1544559 A1 .
  • EP 1666824 A1 EP 1672301 A1 .
  • DE 102005028012 A1 .
  • WO 2007033838 A1 WO 2007104449 A1 .
  • EP 1845324 A1 is
  • the "main heat exchanger system” serves to cool feed air in indirect heat exchange with return streams from the distillation column system. It may be formed of one or more parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • the method of the invention belongs to the class of high pressure processes in which the total air in a main air compressor is compressed to well above high pressure column pressure.
  • the system works with a single externally driven machine, namely this main air compressor.
  • the configuration in which the compressed cooled and purified air is split into two streams - turbine stream ("second substream") and inductor stream ("first substream”).
  • the turbine stream is cooled in the heat exchanger and then relaxed in a turbine, for example, to the pressure of the high pressure column and passed into this.
  • the throttle flow is in a booster stage (“compressor"), driven by the turbine, recompressed, passed through the heat exchanger and thereby cooled and is then passed into the rectification section.
  • the invention is therefore based on the object to provide a method of the type mentioned above and a corresponding device, which are economically particularly favorable, especially at a relatively small inductor current ("first partial flow").
  • a recirculation flow which is formed by a part of the first partial flow of air (the throttle flow) guided through the after-compressor, flows in a circle through the after-compressor. This increases the amount of air to be compressed in the booster.
  • the recycle stream is preferably withdrawn at the exit from the main heat exchanger (at the cold end), depressurized in a throttle valve to a pressure slightly higher than the pressure before entry into the reboiler.
  • the relaxed recycle stream is passed through the main heat exchanger and mixed again with the first part stream before entering the reboiler.
  • This recirculation of the inductor current causes the amount of gas to be compressed in the booster stage (the booster) to increase, the pressure ratio being smaller and the booster and turbine volumes match better.
  • a conventional buildable and particularly efficient booster turbine can be used.
  • the heating of the return flow can be carried out up to the warm end of the main heat exchanger or up to an intermediate temperature.
  • the introduction of the recirculation stream into the first partial stream upstream of the postcompressor can in principle also be effected by introducing the recycle stream into the total air stream before it is divided; the "return to the first partial flow" is then performed upstream of the branch of the first partial flow from the second partial flow.
  • the recycle stream is introduced into the first substream immediately before the postcompressor.
  • the system has only a single externally driven compressor, the main air compressor, and only a single expansion machine (turbine). Despite this comparatively simple structure, it is very energy-efficient by the process of the invention.
  • the total air is compressed in the invention to a first air pressure, which is for example 10 to 30 bar and preferably between 10 and 20 bar.
  • the invention also relates to a device according to claim 4.
  • the device according to the invention can be supplemented by device features which correspond to the features of the dependent method claims.
  • Atmospheric air 1 is sucked in via a filter from a main air compressor 3 and compressed there to a first air pressure of about 18 bar.
  • the main air compressor preferably has several stages with intermediate cooling.
  • the compressed total air is then cooled in a pre-cooler 4 and cleaned in a cleaning device 5.
  • the purified feed air 6 is divided under the first air pressure into a first partial flow 7 and a second partial flow 8.
  • approximately 45% of the total air 6 forms the first partial flow 7, the remainder the second partial flow 8.
  • the first partial flow 7 is fed via line 9 to a secondary compressor 10 with aftercooler 11 and further compressed there to a second air pressure of about 28 bar.
  • the booster 10 is formed in one stage.
  • the post-compressed first partial flow 12 is fed to a main heat exchanger 13 at the warm end, where it is cooled and liquefied and finally withdrawn again at the cold end via line 14.
  • Most of the liquefied first substream is introduced via line 15 and throttle valve 16 in the distillation column system for nitrogen-oxygen separation, which has a high pressure column 17, a low pressure column 18 and a main condenser 19, which is designed as a condenser-evaporator.
  • the operating pressures are 5 to 6 bar in the high-pressure column and 1.2 to 1.6 bar in the low-pressure column.
  • a portion of the introduced into the high-pressure column 17 liquid air is removed again via line 20, cooled in a supercooling countercurrent 21 and fed via throttle valve 22 in the low-pressure column 18.
  • the second partial stream 8 of the feed air is cooled in the main heat exchanger 13 only to an intermediate temperature.
  • the cooled second partial flow 23 is introduced into a relaxation machine, which is formed here by a turbine 24.
  • the second air stream is working expanded relaxed to something about high pressure column pressure.
  • the expanded second partial stream 25 is fed in completely gaseous or substantially completely gaseous state of the high-pressure column immediately above the sump.
  • the expansion machine 24 is directly mechanically coupled to the booster compressor 10, in particular sit after-compressor and turbine on a common shaft.
  • Argon portion 30 comprises a split crude argon column and a pure argon column, is fed by an argon transition fraction 31 and provides a liquid pure argon (LAR) product 32. Otherwise, it operates according to known principles.
  • the top nitrogen 33 of the high-pressure column 17 is condensed at least to a part 34 in the main condenser 19.
  • the liquid nitrogen obtained is fed to a first part 36 as reflux to the high-pressure column 17.
  • a second part 37 is cooled in the subcooling countercurrent 21 and fed via throttle valve 38 into the top of the low pressure column 18. At least a part of it is used as a liquid reflux in the low-pressure column 18.
  • an oxygen product stream is produced 39 withdrawn liquid and brought in liquid state to an elevated pressure of about 30 bar.
  • the high-pressure oxygen 41 is vaporized in the main heat exchanger 13 and warmed to approximately ambient temperature. Via line 42, it is finally recovered as an internally compressed pressure oxygen product (GOX-IC).
  • a portion 60 of the warm residual gas 54 can be used as a regeneration gas (regas gas) in the cleaning device 5.
  • liquid argon 32 can be internally compressed from the argon part 30 in a pump 55 and recovered after (pseudo) evaporation via line 56 as gaseous pressure product (GAR-IC).
  • GAR-IC gaseous pressure product
  • a recycle stream 57 is branched off from the liquefied first substream 14, here downstream of the cold end of the main heat exchanger 12.
  • the recycle stream 57 when depressurized in a throttle valve 58 to a pressure of slightly more than 18 bar, returns to the cold end of the main heat exchanger fed and warmed there to an intermediate temperature of 260 K.
  • the warmed recycle stream 59 is finally fed to the first part stream 7 upstream of the post-compressor 10.
  • the booster 10 in FIG. 1 is operated in warm conditions, ie with an inlet temperature no more than 20 K below ambient temperature.
  • FIG. 2 differs from FIG. 1 in that the after-compressor 110 is operated as a cold compressor, that is to say with an inlet temperature which is more than 20 K below the ambient temperature, in the example at 210 ° K.
  • the recirculation flow 159 also becomes at a lower intermediate temperature of approximately 205 K taken from the main heat exchanger 13 and only downstream of the cooling of the first partial flow 107 combined with this.
  • the division into first partial flow 107 and second partial flow 123 takes place here within the main heat exchanger 13.
  • the recompressed first substream 112 is fed to the main heat exchanger 13 at an intermediate temperature.
  • the expansion machine 124 is not only mechanically coupled to the cold booster 110. Rather, there is an additional oil brake 161 on the common shaft (alternative to the oil brake, a generator could also be used).
  • a second turbine 224 is used instead of the oil brake, which is coupled to a generator 261.
  • a dissipative brake for example an oil brake.
  • the first turbine 124 is mechanically connected only to the cold secondary compressor 110.
  • the two turbines 124, 224 each have the same pressures and temperatures at the inlet and outlet.
  • FIG. 4 differs from the previous embodiments in that the recycle stream 357 is branched off from the first part stream already before the cold end of the main heat exchanger, ie at something at a higher temperature, which may not be higher than dew point, in the example under 130 K. Die During the expansion in the throttle valve 358 generated cold can thus contribute to the cooling of feed air in the main heat exchanger 13.
  • the pre-cooling 4 and the cleaning 5 can be performed at a lower pressure than the first air pressure, as in FIG. 5 is shown.
  • the system must then in addition to the main air compressor 403 another externally driven air compressor 463 having the total purified air 462 from this lower air pressure of, for example, 18 bar to the first air pressure recompressed.
  • the air compressor 463 has an aftercooler, which is not shown in the drawing, and may be of one or more stages and may have an intermediate cooling.

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Claims (4)

  1. Procédé destiné à la production d'oxygène sous pression par décomposition à basse température de l'air dans un système de colonnes de distillation destiné à la séparation azote-oxygène, qui comporte une colonne basse pression (17) et une colonne haute pression (18), dans lequel
    - tout l'air chargé (1) est comprimé à une première pression d'air (3; 403, 463), qui se situe au moins 4 bar au-dessus de la pression de service de la colonne haute pression (18),
    - au moins une partie de l'air chargé comprimé (6) est refroidie dans un échangeur de chaleur principal (13),
    - un premier courant partiel (7, 9; 107) de l'air chargé comprimé à la première pression d'air (6) est re-comprimé dans un post-compresseur (10; 110) à une deuxième pression d'air, qui est plus élevée que la première pression d'air,
    - le premier courant partiel re-comprimé (12; 112) est liquéfié ou pseudo-liquéfié dans l'échangeur de chaleur principal et ensuite introduit au moins en partie (15) dans le système de colonnes de distillation pour la séparation azote-oxygène,
    - un deuxième courant partiel (8, 23; 123) de l'air chargé comprimé à la première pression d'air (6) est refroidi dans l'échangeur de chaleur principal (13) à une température intermédiaire et ensuite détendu en fournissant un travail dans une machine de détente (24; 124), la machine de détente (24; 124) entraînant le post-compresseur (10; 110),
    - le deuxième courant partiel détendu (25) est introduit dans le système de colonnes de distillation pour la séparation azote-oxygène,
    - un courant de produit d'oxygène (39) est extrait à l'état liquide hors du système de colonnes de distillation pour la séparation azote-oxygène et porté à l'état liquide à une pression accrue (40), et
    - le courant de produit d'oxygène porté à pression à l'état liquide est vaporisé ou pseudo-vaporisé sous la pression accrue dans l'échangeur de chaleur principal (13) et chauffé et finalement recueilli sous forme de produit d'oxygène sous pression (42), caractérisé en ce que
    - un courant de retour (57; 357) est dévié hors du premier courant partiel (pseudo-)liquéfié (14),
    - on détend le courant de retour (57; 357) dans une soupape d'étranglement (58; 358) et on le chauffe dans l'échangeur de chaleur principal (13) et
    - on ajoute le courant de retour chauffé (59; 159) au premier courant partiel (7; 107) en amont du post-compresseur (10; 110).
  2. Procédé selon la revendication 1, caractérisé en ce que l'on effectue la compression de l'air chargé (1) à la première pression d'air dans un compresseur d'air principal (3).
  3. Procédé selon la revendication 1, caractérisé en ce que l'on effectue la compression de l'air chargé (1) à la première pression d'air dans un compresseur d'air principal (403) et dans un post-compresseur d'air (463).
  4. Dispositif destiné à la production d'oxygène sous pression par décomposition à basse température avec
    - un système de colonnes de distillation pour la séparation azote-oxygène, qui comporte une colonne basse pression (17) et une colonne haute pression (18),
    - avec des moyens destinés à comprimer tout l'air chargé (1) à une première pression d'air comprimé (3; 403, 463), qui se situe au moins 4 bar au-dessus de la pression de service de la colonne haute pression (18),
    - avec un échangeur de chaleur principal (13) destiné à refroidir au moins une partie de l'air chargé comprimé (6),
    - avec un post-compresseur (10; 110) destiné à recomprimer un premier courant partiel (7, 9; 107) de l'air chargé (6) comprimé à la première pression d'air à une deuxième pression d'air, qui est plus élevée que la première pression d'air,
    - avec des moyens destinés à liquéfier ou pseudo-liquéfier le premier courant partiel re-comprimé (12; 112) dans l'échangeur de chaleur principal et avec des moyens destinés à introduire au moins une partie du premier courant partiel (pseudo-)liquéfié dans le système de colonnes de distillation pour la séparation azote-oxygène,
    - avec des moyens destinés à refroidir un deuxième courant partiel (8, 23; 123) de l'air chargé (6) comprimé à la première pression d'air à une température intermédiaire dans l'échangeur de chaleur principal (13),
    - avec une machine de détente (24; 124) destinée à détendre le deuxième courant partiel refroidi en fournissant un travail, la machine de détente (24; 124) étant mécaniquement couplée au post-compresseur (10; 110),
    - avec des moyens pour introduire le deuxième courant partiel détendu (25) dans le système de colonnes de distillation pour la séparation azote-oxygène,
    - avec des moyens pour extraire un courant de produit d'oxygène (39) à l'état liquide hors du système de colonnes de distillation pour la séparation azote-oxygène,
    - avec des moyens (40) pour l'augmentation de la pression du courant de produit d'oxygène (39) à l'état liquide à une pression accrue, et
    - avec des moyens pour vaporiser ou pseudo-vaporiser et chauffer le courant de produit d'oxygène porté à pression à l'état liquide sous la pression accrue dans l'échangeur de chaleur principal (13) et pour recueillir le courant de produit d'oxygène comme produit d'oxygène sous pression (42),
    caractérisé par
    - des moyens pour dévier un courant de retour (57; 357) hors du premier courant partiel (pseudo-)liquéfié (14),
    - une soupape d'étranglement (58; 358) pour détendre le courant de retour (57; 357),
    - des moyens pour chauffer le courant de retour détendu dans l'échangeur de chaleur principal (13), et par
    - des moyens pour ajouter le courant de retour chauffé (59; 159) au premier courant partiel (7; 107) en amont du post-compresseur (10; 110).
EP12007828.2A 2011-12-01 2012-11-20 Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air Not-in-force EP2600090B1 (fr)

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DE10217091A1 (de) 2002-04-17 2003-11-06 Linde Ag Drei-Säulen-System zur Tieftemperatur-Luftzerlegung mit Argongewinnung
DE10238282A1 (de) 2002-08-21 2003-05-28 Linde Ag Verfahren zur Tieftemperatur-Zerlegung von Luft
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EP1544559A1 (fr) 2003-12-20 2005-06-22 Linde AG Procédé et dispositif pour la séparation cryogénique d'air
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EP1666823A1 (fr) 2004-12-03 2006-06-07 Linde Aktiengesellschaft Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air
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DE102005028012A1 (de) 2005-06-16 2006-09-14 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
WO2007033838A1 (fr) 2005-09-23 2007-03-29 Linde Aktiengesellschaft Procede et dispositif pour analyser la temperature de l'air
DE102006012241A1 (de) * 2006-03-15 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP1845323A1 (fr) 2006-04-13 2007-10-17 Linde Aktiengesellschaft Procédé et dispositif de production d'un produit sous haute pression par séparation cryogénique d'air
DE102006032731A1 (de) 2006-07-14 2007-01-18 Linde Ag Verfahren und Anlage zur Luftzerlegung
EP1892490A1 (fr) 2006-08-16 2008-02-27 Linde Aktiengesellschaft Procédé et dispositif de production variable d'un produit comprimé par séparation cryogénique d'un gaz
DE102007014643A1 (de) 2007-03-27 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
DE102007031759A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
DE102007031765A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
EP2026024A1 (fr) 2007-07-30 2009-02-18 Linde Aktiengesellschaft Procédé et dispositif pour la production d'argon par séparation cryogénique d'air
KR101541742B1 (ko) 2008-01-28 2015-08-04 린데 악티엔게젤샤프트 저온 공기 분리 방법 및 장치
DE102008016355A1 (de) 2008-03-29 2009-10-01 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
WO2011018207A2 (fr) * 2009-08-11 2011-02-17 Linde Aktiengesellschaft Procédé et dispositif pour générer un produit gazeux sous pression contenant de l'oxygène par fractionnement cryogénique de l'air
DE102009048456A1 (de) * 2009-09-21 2011-03-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

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