EP3410050B1 - Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air - Google Patents

Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air Download PDF

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Publication number
EP3410050B1
EP3410050B1 EP18020214.5A EP18020214A EP3410050B1 EP 3410050 B1 EP3410050 B1 EP 3410050B1 EP 18020214 A EP18020214 A EP 18020214A EP 3410050 B1 EP3410050 B1 EP 3410050B1
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Prior art keywords
pressure
column
level
pressure level
booster
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EP18020214.5A
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German (de)
English (en)
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EP3410050A1 (fr
Inventor
Dimitri GOLUBEV
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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
    • F25J3/04048—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
    • F25J3/0406—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
    • F25J3/04915—Combinations of different material exchange elements, e.g. within different columns
    • 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
    • F25J3/04024—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 purified feed air, so-called boosted 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
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • 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
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
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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
    • F25J3/04642—Recovering noble gases from air
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    • F25J3/04654—Producing crude argon in a crude argon column
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    • 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
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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
    • F25J3/04642—Recovering noble gases from air
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    • 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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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/92—Details relating to the feed point
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being oxygen

Definitions

  • the invention relates to a method for obtaining one or more air products and an air separation plant according to the preambles of the independent claims.
  • cryogenic separation of air in air separation plants is known and, for example at H.-W. Haring (ed.), Industrial Gases Processing, Wiley-VCH, 2006 , in particular Section 2.2.5, "Cryogenic Rectification" described.
  • Air separation plants have rectification column systems, which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
  • rectification column systems which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
  • rectification columns for the production of nitrogen and / or oxygen in the liquid and / or gaseous state ie the rectification columns for nitrogen-oxygen separation
  • rectification columns for obtaining further air components in particular the noble gases krypton, xenon and / or argon, can be provided.
  • the rectification columns of said rectification column systems are operated at different pressure levels.
  • Double column systems have a so-called high-pressure column (also referred to as pressure column, medium-pressure column or lower column) and a so-called low-pressure column (also referred to as the upper column).
  • the pressure level of the high pressure column is for example 4 to 6 bar, preferably about 5.5 bar.
  • the low-pressure column is operated at a pressure level of, for example, 1.3 to 1.7 bar, preferably about 1.5 bar.
  • the pressure levels given here and below are in each case absolute pressures that are present at the top of the respectively named columns. The values mentioned are only examples that can be changed if necessary.
  • main compressor / compressor Main Air Compressor / Booster Air Compressor, MAC-BAC
  • HAP high air pressure
  • the total amount of feed air supplied to the rectification column system is compressed to a pressure level which is substantially, ie at least 3, 4, 5, 6, 7, 8, 9 or 10 bar above the pressure level of the high-pressure column.
  • the pressure difference can be, for example, up to 14, 16, 18 or 20 bar.
  • High-pressure methods are for example from the EP 2 980 514 A1 and the EP 2 963 367 A1 known.
  • the present invention is used in particular in air separation plants with so-called internal compression (IV, Internal Compression, IC).
  • IV Internal Compression, IC
  • at least one product which is provided by means of the air separation plant is formed by removing a cryogenic liquid from the rectification column system, subjecting it to a pressure increase, and converting it to the gaseous or supercritical state by heating.
  • internally compressed gaseous oxygen (GOX IV, GOX IC) or nitrogen (GAN IV, GAN IC) can be produced in this way.
  • the internal compression offers a number of advantages over an alternatively also possible external compression and is eg in Häring (see above), Section 2.2.5.2, "Internal Compression", explained. Also for example in the US 2004/0221612 A1 and the US 5,475,980 A internal compression methods are disclosed.
  • high pressure air pressure systems can be an advantageous alternative to the more conventional main compressor / re-compressor processes.
  • the present invention therefore has as its object, at least in some of such cases, to enable an advantageous use of a high-pressure method.
  • the term “amount of feed air” or “feed air” is understood as meaning the total air supplied to the rectification column system of an air separation plant and thus all the air supplied to the rectification column system.
  • a corresponding quantity of feed air in a main compressor / secondary compressor process is only partially compressed to a pressure level which is significantly above the pressure level of the high-pressure column.
  • the total amount of feed air is compressed to such a high pressure level.
  • a “cryogenic” liquid is understood here to mean a liquid medium whose boiling point is significantly below the ambient temperature, for example at -50 ° C. or less, in particular at -100 ° C. or less.
  • Examples of deep-frozen liquids are liquid air, liquid oxygen, liquid nitrogen, liquid argon or liquids that are rich in the compounds mentioned.
  • turbocompressors In air separation plants, multi-stage turbocompressors are used for compressing the amount of feed air, which are referred to here as "main air compressors".
  • the mechanical design of turbocompressors is known in principle to the person skilled in the art.
  • a turbocompressor the compression of the medium to be compressed takes place by means of turbine blades, which are arranged on a turbine wheel or directly on a shaft.
  • a turbocompressor forms a structural unit which, however, can have several compressor stages in a multi-stage turbocompressor.
  • a compressor stage comprises a turbine wheel or a corresponding arrangement of turbine blades. All of these compressor stages can be driven by a common shaft. However, it can also be provided to drive the compressor stages in groups with different waves, wherein the waves can also be connected to each other via gears.
  • the main air compressor is also distinguished by the fact that through this the total amount of air fed into the rectification column system and used for the production of air products, ie the total feed air, is compressed. Accordingly, a "re-compressor" may be provided, but in which only a part of the compressed in the main air compressor air quantity is brought to an even higher pressure.
  • This can also be designed turbocompressors. For compressing partial air quantities, further turbocompressors are typically provided, which are also referred to as boosters, but make only a relatively small amount of compaction compared to the main air compressor or the booster compressor. Even in a high-pressure method, a booster may be present, but this compresses a subset of the air then starting from a correspondingly higher pressure level.
  • turboexpanders can also be coupled with turbo compressors and drive them. If one or more turbocompressors without externally supplied energy, i. driven only by one or more turboexpander, the term "turbine booster" is 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 (for example via a common shaft) or at different speeds (for example via an intermediate gearbox).
  • a booster can basically also be driven using external energy, for example using an electric motor.
  • turbine boosters and booster driven using external energy can be used.
  • Liquid, gaseous or supercritical state fluids may be rich or poor in one or more components as used herein, with “rich” for a content of at least 75%, 90%, 95%, 99%, 99.5%. , 99.9% or 99.99% and “poor” for a content of at most 25%, 10%, 5%, 1%, 0.1% or 0.01% on a molar, weight or volume basis ,
  • the term “predominantly” may correspond to the definition of "rich” just mentioned, but in particular denotes a content of more than 90%. If, for example, "nitrogen” is mentioned here, it can be a pure gas or a nitrogen-rich gas.
  • pressure level and "temperature level” will be used to characterize pressures and temperatures, thereby indicating that pressures and temperatures need not be used in the form of exact pressure or temperature values to achieve an inventive concept.
  • pressures and temperatures typically range in certain ranges that are, for example, ⁇ 1%, 5%, 10%, 20% or even 50% about an average.
  • Different pressure levels and temperature levels can be in disjoint areas or in areas that overlap each other.
  • pressure levels include unavoidable or expected pressure losses, for example due to cooling effects, a.
  • the pressure levels specified here in bar are absolute pressures.
  • the present invention relates, for example, to a method in which about 37,000 standard cubic meters of compressed gaseous oxygen per hour at 31 bar , 20,000 standard cubic meters of gaseous nitrogen per hour at 10 bar, 3,000 standard cubic meters of liquid nitrogen per hour and 3,300 standard cubic meters of liquid oxygen per hour with simultaneous argon production can be formed.
  • a so-called cold booster is used to increase the process efficiency by converting excess cooling capacity into higher air pressure.
  • a corresponding cold booster is conventionally a part of the air separation plant supplied feed air, which has been cooled in the main heat exchanger to an intermediate temperature level and possibly previously been increased in pressure, brought to a higher pressure level.
  • An air separation plant with a cold booster is for example in the EP 3 101 374 A2 disclosed.
  • a booster here is understood to mean a booster which is supplied with fluid which is present at a temperature level which is significantly below the respective ambient temperature at the location of the air separation plant, in particular clearly below 0 ° C., -10 ° C., -20 ° C, -30 ° C, -40 ° C or -50 ° C or below.
  • the increase of the process efficiency by a cold booster is possible, because due to the comparatively reduced liquid power the system no corresponding amount of refrigerant is "withdrawn", as would be the case if corresponding products were made liquid.
  • a cold booster for use in the present invention may be designed as a turbine booster or as a booster powered by external energy.
  • the kF value (ie the product of heat transfer coefficient k and heat exchanger surface F) of the main heat exchanger of an air separation plant can be increased by the use of a cold booster. This is due to the fact that the power absorbed in the cold booster during the cold compression is dissipated virtually completely in the main heat exchanger itself. Although this improves the internal compression process or the QT profile in the heat exchanger, the required exchange surface area becomes larger because the amount of compressed gas in a specific temperature range is cooled virtually twice. To illustrate, for example, on FIG. 1 the already mentioned EP 3 101 374 A2 pointed.
  • the stream i is due to the increase in temperature by the compression of the main heat exchanger 7 taken before the pressure increase in the cold booster 101 at a lower temperature level than that on which it is then fed back to the main heat exchanger 7.
  • the improvement in the QT profile is thermodynamically due to the increase in the difference in heat capacities of the cold and warm streams in this temperature range.
  • An improvement in the efficiency of high-pressure air method by the use of multiple throttle currents at different pressures is also known.
  • An "inductor flow” is a part of the amount of feed air cooled at a pressure level above the operating pressure of the high pressure column in the main heat exchanger, at least partially liquefied or converted at the appropriate pressure on the gaseous in the supercritical state and then by means of a relaxation device, classically relaxed an expansion valve ("throttle") and the rectification column system, in particular the high-pressure column, is supplied.
  • a pressure nitrogen product for example, about 10 bar, for example, can be provided by re-densification, in particular as pressure nitrogen from the at 5.5 bar working high-pressure column or by internal compression.
  • re-densification in particular as pressure nitrogen from the at 5.5 bar working high-pressure column or by internal compression.
  • a separate compressor is required, in the latter case an internal compression pump and an even larger heat exchanger.
  • the object explained at the outset which is to provide a cost-effective and nevertheless efficient HAP process, is achieved in that, instead of cold compaction of an incoming air stream for improving the QT profile in the main heat exchanger, as is fundamentally up to date It is known in the art to cold compress a stream of nitrogen from the high pressure column in a turbine booster or booster powered by external energy. This is configured in the context of the present invention in a particularly advantageous manner and further developed.
  • the pressure ratios of cold booster are typically at most 1.9 to 2.
  • a pressure ratio is defined as the ratio of the inlet pressure to the outlet pressure of a corresponding booster. This pressure ratio is sufficient to deliver the required amount of nitrogen product, in the present case at about 10 bar. Therefore, a cold booster for providing pressurized nitrogen at a corresponding pressure level is advantageously used.
  • a cold booster for a corresponding nitrogen product stream basically the same effect can be achieved as by the cold compression in the cold booster and the subsequent cooling of a partial flow of the feed air.
  • the improvement in the QT profile is also achieved by the more favorable ratio of heat capacities between the cold and warm streams.
  • the difference is that in the embodiment proposed in the present invention, the heat capacity of cold streams (by diverting a corresponding nitrogen flow to the cold booster) is reduced in certain heat exchanger areas.
  • the heat capacity of hot streams is increased by a double guiding of the cold-compressed air stream through the heat exchanger. The difference described has a positive effect on the kF value of the heat exchanger.
  • the performance of the cold booster for the pressurized nitrogen is not in the main heat exchanger must be removed (the pressurized nitrogen stream heats up through the compression and is then fed back to the main heat exchanger at a suitable location for subsequent heating to near ambient temperature).
  • the present invention in addition to the cold compression of a pressurized nitrogen product, also includes the particularly advantageous balancing of the excess cooling capacity throughout the process and the performance of the cold booster.
  • This can be achieved in that in a particularly preferred embodiment of the invention, in addition to the amount of product, a certain additional amount of pressurized nitrogen from the high-pressure column is also compressed and then used as an additional inductor current in the main heat exchanger. A corresponding additional amount of pressurized nitrogen is thus at least partially liquefied in the main heat exchanger and fed back into the rectification column system, in particular the high-pressure column.
  • this design is a combination of both described methods for improving the QT profile.
  • the use of an additional nitrogen restrictor flow also has a positive effect on the product yield, since less air is pre-liquefied in this way (instead of feed air, pressurized nitrogen liquefied from the high pressure column).
  • the low-pressure column should be carried out with argon optimization, ie with an additional rectification section between the feed points of the argon condensers, if, for example, crude and pure argon columns or argon discharge columns are used.
  • the amount of additional nitrogen flow is thereby an optimization parameter. All nitrogen taken from the high pressure column and neither condensed nor recycled as reflux into it nor condensed and used as a liquid reflux to the low pressure column (as in the present case), basically affects the Separation in the low-pressure column because he is no longer available there as a return.
  • the present invention proposes a method for recovering one or more air products using an air separation plant having a rectification column system comprising a high pressure column and a low pressure column, and further equipped with a main heat exchanger and a main air compressor.
  • the present invention is used in connection with a high-pressure method, so it is the entire, the rectification column system supplied air in the main compressor compressed to a first pressure level and the high-pressure column is operated at a second pressure level, which is at least 3 bar is below the first pressure level.
  • a second pressure level which is at least 3 bar is below the first pressure level.
  • the gaseous, nitrogen-rich fluid is taken from the high-pressure column at the second pressure level and heated in the gaseous state without prior liquefaction.
  • This fluid is in conventional air separation plants to pressurized nitrogen, which is to be withdrawn as a process product of the air separation plant.
  • pressurized nitrogen which is to be withdrawn as a process product of the air separation plant.
  • complete heating of such nitrogen-rich fluid in the main heat exchanger and subsequent delivery as a corresponding product occurs. If this is referred to, that a corresponding fluid is heated "in the gaseous state" without a prior liquefaction, it is to be understood here that a corresponding fluid is not nitrogen taken from the high-pressure column, in a high-pressure column.
  • such fluid can basically be warmed or serve, for example, to provide liquid nitrogen.
  • Corresponding fluids can also be used in the context of the present invention (but in addition to the fluid heated in the gaseous state without prior liquefaction).
  • a first subset of the gaseous, nitrogen-rich fluid to a first temperature level of -150 to -100 ° C, in particular from -140 to -120 ° C, for example -130 ° C, to warm up to a booster at this first temperature level, and continue to compress to a third pressure level using the booster.
  • the booster because of the temperature levels at which the gaseous, nitrogen-rich fluid or the first subset of this fluid are supplied to the booster, is a "cold booster" in the sense explained above. This can be designed as a turbine booster or as a booster powered by external energy, as already explained. The benefits of using a cold booster have also been previously mentioned.
  • the third pressure level is in particular at a pressure level at which a corresponding nitrogen product is to be delivered, for example at a pressure of 8 to 12 bar, in particular from 9 to 11 bar, for example 10 bar.
  • a pressure level is thus the discharge pressure of a corresponding nitrogen-rich printed product.
  • the first subset is further provided to heat the first subset after compression to the third pressure level to a second temperature level above the first temperature level, which may be in particular at ambient temperature, and to discharge it permanently from the air separation plant.
  • the corresponding first subset is thus provided as a printed product.
  • the present invention also to heat a second subset of the gaseous, nitrogen-rich fluid together with the previously mentioned first subset to the first temperature level, at this first temperature level to the booster, and continue using the booster to compress to the third pressure level.
  • it is provided to cool the second subset after compression to the third pressure level to a third temperature level below the first temperature level, then to relax to the second pressure level and return the high pressure column.
  • the second subset is in particular at least partially liquefied or transferred from the supercritical state into the liquid state.
  • the third temperature level may be a temperature level of -180 to -165 ° C, in particular of -177 to -167 ° C, for example -172 ° C, act.
  • the present invention also possible to heat a third portion of the nitrogen-rich fluid without compression to the third pressure level to the first temperature level and permanently divert from the air separation plant.
  • Corresponding nitrogen can be provided for example in the form of so-called seal gas or as a nitrogen product at a lower pressure level.
  • the first, the second and the third subset preferably together form the total amount of the high-pressure column removed and non-liquefied nitrogen-rich fluid.
  • the first and the second subset are heated to the first temperature level using the main heat exchanger, and / or if the first subset is heated to the second temperature level using the main heat exchanger and / or if the first subset second subset is cooled using the main heat exchanger to the third temperature level.
  • the Q-T profile and the kF value of the main heat exchanger can be influenced in a particularly favorable manner.
  • the booster used for compression of the cold nitrogen flow so the cold booster, in one embodiment of the present invention, as mentioned, coupled with an expansion turbine, so represents a turbine booster.
  • a Part of the rectification column system supplied air to the second pressure level is relaxed, which was previously cooled using the main air compressor to a fourth temperature level and which is then fed into the high-pressure column.
  • the fourth temperature level may be -170 to -120 ° C, especially at -160 to -130 ° C, for example -149 ° C.
  • the relaxation of part of the air supplied to the rectification system in an expansion turbine in order to drive the cold booster can in principle also take place at approximately the pressure level of the low-pressure column with subsequent introduction of this flow into the low-pressure column.
  • the cold booster may be powered using external energy, not energy stored in a process stream provided in the air separation plant.
  • an electric motor can be used for driving the cold booster.
  • the second subset comprises a fraction, in particular a standardized fraction, for example expressed in standard cubic meters per hour, from 0 to 60%, in particular from 10 to 50%, for example from 15 to 35%, of the high-pressure column on the second Pressure taken and heated without prior liquefaction in the gaseous state gaseous nitrogen-rich fluid.
  • a fraction in particular a standardized fraction, for example expressed in standard cubic meters per hour, from 0 to 60%, in particular from 10 to 50%, for example from 15 to 35%, of the high-pressure column on the second Pressure taken and heated without prior liquefaction in the gaseous state gaseous nitrogen-rich fluid.
  • a part of the air supplied to the rectification column system is compressed in a further booster from the first pressure level to a fifth pressure level of 20 to 30 bar, in particular 22 to 27 bar, for example 25 bar, using the main heat exchanger cooled to a fifth temperature level, expanded in a mechanically coupled with the further booster expansion turbine to the second pressure level, and then fed into the high-pressure column.
  • a so-called warm booster can basically correspond to the prior art and supports the achievable within the scope of the present invention advantages.
  • a sixth temperature level for example - 165 to -115 ° C, especially at -150 to -130 ° C, for example -141 ° C
  • the rectification column system comprises at least one rectification column into which a first fluid enriched in argon with respect to a bottom liquid of the high-pressure column is transferred from the low-pressure column, and in which the first fluid is depleted of argon. An after depletion of argon remaining remainder of the first fluid is thereby recycled in the form of a second fluid in the low pressure column.
  • the present invention can be used in principle using known crude and possibly pure argon columns, but it is also a pure Argonausschleusung without obtaining an argon product using so-called Argonausschleuskla possible.
  • the advantageous effect of the resulting Argonausschleusung from the separated in the low pressure column fluid is due to the fact that the oxygen-argon separation for the discharged argon in the low-pressure column is no longer necessary.
  • the separation of the argon from the oxygen in the low pressure column itself is basically expensive and requires a corresponding "heating" performance of the main capacitor. If argon is discharged and thus omits the oxygen-argon separation or this is displaced, for example, in a crude argon or Argonausschleuskla, the corresponding amount of argon must not be separated in the oxygen section of the low pressure column and the heating power of the main capacitor can be reduced. Therefore, with the same yield of oxygen, more pressure nitrogen can be removed from the high-pressure column, which is currently the goal of the present invention.
  • an "argon discharge column” can be understood to mean a separation column for the argon-oxygen separation, which does not serve to obtain a pure argon product but to remove argon from the air to be separated in the high-pressure column and low-pressure column.
  • Their circuit differs only slightly from that of a conventional crude argon column, but it contains significantly less theoretical plates, namely less than 40, especially between 15 and 30.
  • an argon discharge column Like a crude argon column, the bottom region of an argon discharge column is connected to an intermediate point of the low pressure column and the argon discharge column is passed through cooled a top condenser, on its evaporation side typically relaxed bottoms liquid from the high pressure column is introduced.
  • An argon discharge column typically does not have a bottom evaporator.
  • a crude and a pure argon column are used, which are each operated with a top condenser, in which oxygen-enriched liquid from the bottom of the high-pressure column, which is in particular previously passed through a supercooling countercurrent, partially evaporated.
  • An unevaporated portion is fed in each case liquid into the low-pressure column.
  • the feeding of the unevaporated fraction from the top condenser of the pure argon column is advantageously carried out 5 to 15 theoretical plates above the feed of the unevaporated fraction from the top condenser of the crude argon column and the latter again above the removal of the first and the return of the second fluid. In this way, an "argon-optimized" separation can be achieved, which allows a corresponding removal of larger amount of nitrogen-rich fluid from the high-pressure column.
  • the present invention further relates to a plant for the production of one or more air products, with respect to the features of which reference is made to the corresponding independent claim.
  • FIG. 1 an air separation plant according to an embodiment of the invention is shown in a simplified, schematic representation and designated 100.
  • a feed air flow a (AIR) is sucked in by means of a main air compressor 1 via a filter 2 and compressed to a pressure level, which is referred to here as the first pressure level.
  • the main air compressor 1 may in particular be designed in multiple stages with intermediate cooling.
  • a radiator associated with the main air compressor 1 is shown as representative of a plurality of corresponding radiators and designated 3.
  • the air separation process performed in the air separation plant 100 is a high air pressure process as discussed above, such that the first pressure level is at least 3 bar above a pressure level on which a high pressure column 14 of a rectification column system (see below) of the air separation plant 100 is operated, secondarily here Pressure level is called.
  • the total amount of air supplied to the rectification column system, which is compressed to the first pressure level, is referred to herein as the amount of feed air.
  • This amount of feed air is first cooled in the form of the feed air stream a in a cooling device 4 and then at least largely freed of water and carbon dioxide in an adsorption device 5.
  • the cooling device 4 is operated in the manner shown with cooling water (H2O), regenerates the adsorption 5 with regeneration gas, which can be delivered after its use to the atmosphere (ATM).
  • the cooled and purified feed air stream a now designated b for better distinctness, is first divided into two partial streams c and d.
  • the partial flow c is brought in a booster 6, which is mechanically coupled to an expansion turbine 7, to a pressure level above the first pressure level and after cooling in an aftercooler again divided into two partial flows e and f, which are fed to a main heat exchanger 9 of the air separation plant 100 , Since the partial flow e is the booster 6 at ambient temperature or above, but in any case at a temperature level above 0 ° C, fed, it is also referred to as a warm booster.
  • the partial flow e is taken from the main heat exchanger 9 at an intermediate temperature level, expanded in the expansion turbine 7 and fed into the high-pressure column 14 in at least partially gaseous state.
  • the partial flow f is removed from the main heat exchanger 9 cold side and fed via a throttle 10 in the liquid state in the high-pressure column 14. The partial flow f is thus a first throttle flow.
  • the partial flow c is also divided again into two partial flows g and h, which are fed to the main heat exchanger 9 of the air separation plant 100.
  • the partial flow g is taken from the main heat exchanger 9 at an intermediate temperature level, in an expansion turbine 11, which is mechanically coupled to a booster 12, relaxed and in at least partially gaseous state, the high-pressure column 14 is fed. He is previously united with the partial flow e. Since the booster 12, as explained below, fluid significantly below ambient temperature, but definitely below 0 ° C, -10 ° C, -20 ° C, -30 ° C, -40 ° C, -50 ° C, is supplied, He is also referred to as a cold booster.
  • the partial flow h is removed from the main heat exchanger 9 on the cold side and fed via a throttle 13 in the liquid state into the high-pressure column 14. It is previously combined with the partial flow f or fed directly into the high-pressure column 14. The partial flow h is therefore a second throttle flow.
  • the operation of the rectification column system comprising in the desalination plant 100 the already mentioned high-pressure column 14, a low-pressure column 15, a crude argon column 16 and a pure argon column 17 can basically be taken from the technical literature cited above.
  • the air separation plant 100 is set up for internal compression.
  • the low-pressure column 15 is taken from an oxygen-rich bottom product in the form of a stream i liquid, to a proportion in the form of a stream k in an internal compression pump 18 to about 30 bar (a) or to a higher, for example to a supercritical, pressure level brought vaporized in the main heat exchanger 9 and transferred from the liquid to the supercritical state, and delivered as internally compressed oxygen-rich air product (GOX IC) at the plant boundary.
  • Another portion of the stream i is not internally compressed, but instead conducted in the form of a stream I to the plant boundary and there delivered as a liquid oxygen product (LOX).
  • the temperature can be adjusted by a partial guiding of the material flow I through a subcooling countercurrent 19.
  • Oxygen-enriched liquid in the form of a stream m can be taken from the bottom of the high-pressure column 14.
  • the stream m can be passed through the subcooling countercurrent 19 and then proportionally fed into the respective evaporation chambers of the top condensers of the crude argon column 16 and the pure argon column 17.
  • liquid and gaseous components are fed into the low-pressure column 15.
  • the crude argon column 16 and the pure argon column 17 are operated in a known manner.
  • an argon-enriched fluid in the form of a stream n is removed from the low-pressure column 15 at a suitable position and depleted of oxygen in the crude argon column 16, which is returned to the low-pressure column 15.
  • Nitrogenous crude argon is transferred in the form of a stream o in the pure argon column, where in particular nitrogen can be separated and released into the atmosphere (ATM).
  • Liquid argon (LAR) can be delivered as a product at the plant boundary.
  • the low-pressure column 15 can be taken from the top side gas, which in the form of a stream p through the supercooling countercurrent 19 and then passed through the main heat exchanger 9 (see also linkage A) and partly after heating in a heater 20 as the aforementioned regeneration in the adsorption 5 can be used. Also, a discharge to the atmosphere (ATM), for example, at times when no regeneration gas is needed, is basically possible. From a bottom in an upper region of the low pressure column 15, a liquid, nitrogen-rich stream q can be withdrawn and discharged as a liquid product (LIN) at the plant boundary.
  • LIN liquid product
  • Liquid air can be withdrawn from the high-pressure column 14 in the form of a stream of material r, passed through the subcooling countercurrent 19 and fed into the low-pressure column 15.
  • nitrogen-rich gas can be withdrawn in the form of a stream s. This can be liquefied to a part in the form of a stream t in a high pressure column 14 and the low pressure column 15 heat-exchanging main condenser 21 and used as reflux to the high pressure column 14 and passed through the subcooling countercurrent 19 and fed into the low pressure column 15.
  • An essential aspect of the present invention in the illustrated embodiment is the treatment of the portion of the stream s not passed through the main condenser 21. This is because it was taken from the high-pressure column, at its pressure level, the second pressure level, before, and in the example shown in the form of a stream u the main heat exchanger. 9 supplied cold side. A partial flow v is removed from the main heat exchanger 9 on the warm side and provided, for example, as a sealing gas (seal gas).
  • Another substream w is taken from the main heat exchanger 9 at an intermediate temperature level, which is referred to herein as the first temperature level, and brought to a pressure level above the second pressure level in the aforementioned booster 12, referred to herein as the third pressure level.
  • a partial flow x of the partial flow w is again supplied to the main heat exchanger 9, this cold side taken, that is cooled to a temperature level, which is referred to here as the third temperature level, relaxed in the liquid state via a throttle 22 and returned to an upper region of the high pressure column 14.
  • the partial flow x is thus another throttle flow.
  • a further partial flow y of the partial flow w is heated in the main heat exchanger 9 to a temperature level, which is referred to here as the second temperature level, and discharged at the system boundary as gaseous pressure nitrogen product.
  • the high pressure column 15 is removed in the form of a stream u at the second pressure level and heated using the main heat exchanger 9, using the main heat exchanger. 9 heated to the first temperature level, supplied to the booster 12 thereon, and further compressed using the booster 12 to the third pressure level.
  • the first subset i. the stream y
  • the second subset i. the stream x
  • the second subset is cooled after compression to the third pressure level using the main heat exchanger 9 to the third temperature level, relaxed to the second pressure level and returned to the high-pressure column 15.
  • FIG. 2 shows an air separation plant according to a further embodiment of the invention in a schematic representation, with a description already to figure 1 explained components is omitted. These are not provided again with reference numerals.
  • a portion of the liquefied in the main condenser 21 nitrogen-rich gas comparable to the stream k according to Appendix 100 or FIG. 1 (see link X in FIG. 2 ), also compressed by means of a further internal compression pump 201, heated in the main heat exchanger 9 and then provided as internally compressed, gaseous nitrogen product (GAN IC).
  • GAN IC gaseous nitrogen product
  • FIG. 3 shows an air separation plant according to a further embodiment of the invention in a schematic representation. Again, a description has already been added FIG. 1 or 2 explained components omitted. These are not provided again with reference numerals.
  • FIG. 4 shows an air separation plant according to a further embodiment of the invention in a schematic representation.
  • a description has already been omitted here to the previous figures explained components, which are not again provided with reference numerals here.
  • the booster 12 can also be driven using external energy, for example using an electric motor M. In this way, it is possible to use the separate provision of a material flow g (FIG. FIG. 1 ) or 301 ( FIG. 3 ) are waived.

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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)

Claims (14)

  1. Procédé de récupération d'au moins un produit à base d'air à l'aide d'une installation de séparation d'air (100) équipée d'un système de colonnes de rectification (14 à 17) qui comporte une colonne à haute pression (14) et une colonne à basse pression (15), ainsi que d'un échangeur de chaleur principal (9) et d'un compresseur d'air principal (1), procédé dans lequel
    - la totalité de l'air amené au système de colonnes de rectification (14 à 17) du compresseur d'air principal (1) est comprimé à un premier niveau de pression, la colonne à haute pression (15) étant utilisée à un deuxième niveau de pression situé à au moins 3 bars au-dessous du premier niveau de pression, et
    - un fluide riche en azote gazeux est retiré de la colonne à haute pression (15) mise au deuxième niveau de pression, et est chauffé à l'état gazeux sans liquéfaction préalable,
    caractérisé en ce que
    - une première fraction du fluide riche en azote gazeux est chauffée à un premier niveau de température dans la gamme de -150 à -100°C, en particulier de -140 à -120 °C, amenée à un surpresseur (12) à ce premier niveau de température et est comprimée à un troisième niveau de pression à l'aide de ce surpresseur (12), et
    - la première fraction est chauffée, après la compression au troisième niveau de pression, à un deuxième niveau de température supérieur au premier niveau de température et est évacuée en permanence de l'installation de séparation d'air (100).
  2. Procédé selon la revendication 1, dans lequel une deuxième fraction du fluide riche en azote gazeux est chauffée conjointement avec la première fraction au premier niveau de température, est amenée au surpresseur (12), puis est encore comprimée au troisième niveau de pression à l'aide du surpresseur (12), la deuxième fraction étant refroidie, après la compression au troisième niveau de pression, à un troisième niveau de température inférieur au premier niveau de température, puis étant détendue au deuxième niveau de pression et renvoyée dans la colonne à haute pression (15) .
  3. Procédé selon la revendication 2, dans lequel une troisième fraction du fluide riche en azote est chauffée au premier niveau de température sans compression au troisième niveau de pression et évacuée en permanence de l'installation de séparation d'air (100) .
  4. Procédé selon la revendication 2 ou 3, dans lequel les première et deuxième fractions sont chauffées au premier niveau de température à l'aide de l'échangeur de chaleur principal (9) et/ou la première fraction est chauffée au deuxième niveau de température à l'aide de l'échangeur de chaleur principal (9), et/ou dans lequel la deuxième fraction est refroidie au troisième niveau de température à l'aide de l'échangeur de chaleur principal (9).
  5. Procédé selon l'une des revendications précédentes, dans lequel le troisième niveau de pression est compris entre 8 et 12 bars.
  6. Procédé selon l'une des revendications précédentes, dans lequel le surpresseur (12) est accouplé mécaniquement à une turbine de détente (11), en particulier une partie de l'air amené au système de colonnes de rectification (14 à 17) est détendue au second niveau de pression dans la turbine de détente (11) accouplée au surpresseur (12), laquelle partie a été préalablement refroidie à un quatrième niveau de température à l'aide du compresseur d'air principal (9), puis est amenée à la colonne à haute pression (14) .
  7. Procédé selon l'une des revendications 1 à 5, dans lequel le surpresseur (12) est entraîné par de l'énergie extérieure, notamment au moyen d'un moteur électrique (M).
  8. Procédé selon la revendication 2 ou l'une des revendications dépendantes de la revendication 2, dans lequel la deuxième fraction comprend une proportion de 10 à 50 % du fluide riche en azote gazeux retiré de la colonne à haute pression (15) au deuxième niveau de pression et chauffé à l'état gazeux sans liquéfaction préalable.
  9. Procédé selon l'une des revendications précédentes, dans lequel une partie de l'air amené au système de colonnes de rectification (14 à 17) est comprimée du premier niveau de pression à un cinquième niveau de pression dans un autre surpresseur (6), est refroidie à un cinquième niveau de température à l'aide de l'échangeur de chaleur principal (9), est détendue au deuxième niveau de pression dans une turbine de détente (7) accouplée mécaniquement à l'autre surpresseur (6) puis introduite dans la colonne à haute pression (14).
  10. Procédé selon la revendication 9, dans lequel une partie de l'air amené au système de colonnes de rectification (14 à 17) est comprimée du premier niveau de pression au cinquième niveau de pression dans l'autre surpresseur (6), est refroidie à un sixième niveau de température à l'aide de l'échangeur de chaleur principal (9), est détendue au deuxième niveau de pression puis introduite dans la colonne à haute pression (14).
  11. Procédé selon l'une des revendications précédentes, dans lequel une partie de l'air amené au système de colonnes de rectification (14 à 17) est refroidie au premier niveau de pression à l'aide de l'échangeur de chaleur principal (9), est détendue du premier niveau de pression au deuxième niveau de pression puis introduite dans la colonne à haute pression (14).
  12. Procédé selon l'une des revendications précédentes, dans lequel le système de colonnes de rectification (14 à 17) comprend au moins une colonne de rectification (16), dans laquelle un fluide enrichi en argon par rapport à un liquide du bas de la colonne à haute pression (15) est transféré depuis la colonne à basse pression (15), et dans lequel le premier fluide est appauvri en argon, un résidu du premier fluide restant après appauvrissement en argon étant renvoyé dans la colonne à basse pression (15).
  13. Procédé selon la revendication 12, dans lequel des colonne d'argon brut et colonne d'argon pur (16, 17) sont utilisées avec des condenseurs de tête dans lesquels un liquide enrichi en oxygène provenant du bas de la colonne à haute pression (14) est partiellement évaporé, une partie non vaporisée provenant du condenseur de tête de la colonne d'argon pur (17) étant renvoyé dans la colonne à basse pression (15) 5 à 15 étages de séparation théoriques au-dessus de l'alimentation de la partie non vaporisée provenant du condenseur de tête de la colonne d'argon brut (16).
  14. Installation de séparation d'air (100) équipée d'un système de colonnes de rectification (14 à 17) qui comporte une colonne à haute pression (14) et une colonne à basse pression (15), ainsi que d'un échangeur de chaleur principal (9) et d'un compresseur d'air principal, l'installation (100) comprenant des moyens adaptés pour
    - comprimer la totalité de l'air amené au système de colonnes de rectification (14 à 17) à un premier niveau de pression dans le compresseur d'air principal (1), la colonne à haute pression (15) étant utilisée à un deuxième niveau de pression situé à au moins 3 bars au-dessous du premier niveau de pression, et
    - retirer un fluide riche en azote gazeux de la colonne à haute pression (15) mise au deuxième niveau de pression, et le chauffer à l'état gazeux sans liquéfaction préalable,
    caractérisée par des moyens adaptés pour
    - chauffer une première fraction du fluide riche en azote gazeux à un premier niveau de température dans la gamme de -150 à -100°C, en particulier de -140 à - 120 °C, l'amener à un surpresseur (12) à ce premier niveau de température et la comprimer à un troisième niveau de pression à l'aide de ce surpresseur (12), et
    - chauffer la première fraction, après la compression au troisième niveau de pression, à un deuxième niveau de température supérieur au premier niveau de température et l'évacuer en permanence de l'installation de séparation d'air (100).
EP18020214.5A 2017-06-02 2018-05-17 Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air Active EP3410050B1 (fr)

Priority Applications (1)

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EP17020238 2017-06-02

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EP (1) EP3410050B1 (fr)
CN (1) CN109059421B (fr)
HU (1) HUE045459T2 (fr)
PL (1) PL3410050T3 (fr)
RU (1) RU2768445C2 (fr)
TR (1) TR201910679T4 (fr)
TW (1) TWI770186B (fr)

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US11635254B2 (en) * 2017-12-28 2023-04-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Utilization of nitrogen-enriched streams produced in air separation units comprising split-core main heat exchangers
WO2019214847A1 (fr) * 2018-05-07 2019-11-14 Linde Aktiengesellschaft Procédé pour produire un ou plusieurs produit(s) formés à partir d'air et installation de séparation d'air
US11566841B2 (en) * 2019-11-27 2023-01-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic liquefier by integration with power plant
US11512897B2 (en) * 2021-01-14 2022-11-29 Air Products And Chemicals, Inc. Fluid recovery process and apparatus

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TWI770186B (zh) 2022-07-11
CN109059421B (zh) 2022-05-31
RU2768445C2 (ru) 2022-03-24
EP3410050A1 (fr) 2018-12-05
CN109059421A (zh) 2018-12-21
US20180347900A1 (en) 2018-12-06
RU2018120350A (ru) 2019-12-03
HUE045459T2 (hu) 2019-12-30
RU2018120350A3 (fr) 2021-11-08
US11098950B2 (en) 2021-08-24
TW201903342A (zh) 2019-01-16
TR201910679T4 (tr) 2019-08-21
PL3410050T3 (pl) 2019-10-31

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