EP3175192A1 - Procédé de séparation cryogénique de l'air et installation de séparation d'air - Google Patents

Procédé de séparation cryogénique de l'air et installation de séparation d'air

Info

Publication number
EP3175192A1
EP3175192A1 EP15742185.0A EP15742185A EP3175192A1 EP 3175192 A1 EP3175192 A1 EP 3175192A1 EP 15742185 A EP15742185 A EP 15742185A EP 3175192 A1 EP3175192 A1 EP 3175192A1
Authority
EP
European Patent Office
Prior art keywords
air
pressure
pressure level
turbine
heat exchanger
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP15742185.0A
Other languages
German (de)
English (en)
Other versions
EP3175192C0 (fr
EP3175192B1 (fr
Inventor
Tobias Lautenschlager
Dimitri GOLUBEV
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP3175192A1 publication Critical patent/EP3175192A1/fr
Application granted granted Critical
Publication of EP3175192C0 publication Critical patent/EP3175192C0/fr
Publication of EP3175192B1 publication Critical patent/EP3175192B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04006—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
    • F25J3/04006—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
    • F25J3/04048—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
    • 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
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04121—Steam turbine as the prime mechanical driver
    • 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
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/04248—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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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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
    • F25J3/04248—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.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J3/04248—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
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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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/40—Separating high boiling, i.e. less volatile components from air, e.g. CO2, hydrocarbons
    • 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
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Definitions

  • the invention relates to a method for the cryogenic separation of air in an air separation plant and a corresponding air separation plant according to the preambles of the independent claims.
  • Air separation plants have distillation 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. In addition to the
  • gaseous oxygen GOX
  • liquid nitrogen LIN
  • Nitrogen, GAN ie the distillation columns for nitrogen-oxygen separation
  • distillation columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • distillation column systems are operated at different operating pressures in their respective distillation columns.
  • Known double column systems have, for example, a so-called high-pressure column (sometimes also referred to as
  • Pressure column called) and a so-called low pressure column.
  • the operating pressure of the high-pressure column is, for example, 4.3 to 6.9 bar, preferably about 5.0 bar.
  • the low pressure column is at an operating pressure of, for example, 1, 3 to 1, 7 bar, preferably about 1, 5 bar, operated.
  • the pressures given here and below are absolute pressures.
  • HAP high-air pressure
  • Distillationsklalensystems typically well above the operating pressure of the high pressure column is.
  • the pressure difference is at least 2 or 4 bar and preferably between 6 and 16 bar.
  • the pressure is at least twice as high as the operating pressure of the high-pressure column.
  • HAP methods are e.g. from EP 2 466 236 A1, EP 2 458 311 A1 and US Pat. No. 5,329,776 A. In HAP processes can be due to the greater compression of the
  • the compressed air quantity in the main air compressor can also be decoupled from the process air quantity.
  • process air so used for the actual rectification and fed into the high-pressure column.
  • process air so used for the actual rectification and fed into the high-pressure column.
  • Another part is relaxed to recover cold, whereby the amount of cold can be adjusted independently of the process air.
  • decoupling is not provided in all HAP methods.
  • Post-compressor are also known as MAC / BAC (Main Air
  • Compressor / Booster Air Compressor In a MAC / BAC process, therefore, not all of the feed air, but only a part is compressed to a pressure well above the highest operating pressure of the distillation column system.
  • the so-called internal compression can be used.
  • a liquid stream is taken from the distillation column system and at least partially brought to liquid pressure.
  • the liquid brought to pressure is heated in a main heat exchanger of the air separation plant against a heat transfer medium and evaporated or, in the presence of appropriate pressures, transferred from the liquid to the supercritical state.
  • the liquid stream may in particular be liquid oxygen, but also nitrogen or argon.
  • the internal compression is thus used to obtain appropriate gaseous printed products.
  • the advantage of internal compression processes is that corresponding fluids do not have to be compressed outside the air separation plant in a gaseous state, which often proves to be very complicated and / or requires considerable safety measures.
  • the internal compression is described in the literature cited above.
  • the collective term "liquefaction" is used for the transfer from the liquid to the supercritical or gaseous state.
  • the transition from the supercritical or gaseous to the liquid state, whose product is a clearly defined liquid, is referred to as "liquefaction”.
  • a heat transfer fluid is liquefied.
  • Heat transfer medium is usually formed by a part of the air separation plant air supplied. In order to efficiently heat and liquefy the stream brought to liquid pressure, this heat transfer medium must be due to
  • thermodynamic conditions have a higher pressure than the fluidly pressurized stream. Therefore, a correspondingly high-density power must be provided.
  • This is also referred to as "throttle flow", because it is conventionally by means of a relaxation valve ("throttle") relaxed, thereby at least partially liquefied and used in the
  • the present invention proposes a method for
  • common wave can be coupled to other expansion turbines or energy converters such as oil brakes, generators or compressors is set up to relax a gaseous or at least partially liquid stream.
  • expansion turbines may be designed for use in the present invention as a turboexpander. If a compressor is driven by one or more expansion turbines, but without externally, for example by means of an electric motor, supplied energy, the term “turbine-driven compressor” or alternatively “turbine booster” is used.
  • a “compressor” is a device that is capable of compressing at least one
  • Compressor is supplied to at least one final pressure at which this the
  • a compressor forms a structural unit, which, however, can have a plurality of “compressor stages” in the form of piston, screw and / or Schaufelrad- or turbine assemblies (ie axial or radial compressor stages). This also applies in particular to the "main (air) compressor” of an air separation plant, which is characterized by the fact that all or most of it is fed into the air separation plant
  • Air quantity ie the total feed air flow
  • a "secondary compressor” in which a part of the air quantity compressed in the main air compressor is brought to an even higher pressure in the MAC / BAC process, is often also of multi-stage design.
  • corresponding compressor stages are driven by means of a common drive, for example via a common shaft.
  • MAC / BAC processes use recompressors that are driven by externally supplied energy; in HAP processes, such recompressors are not.
  • turbine boosters are typically present in both cases, in particular in order to be able to make sensible use of shaft power released during the expansion for cooling purposes.
  • a "heat exchanger" serves for the indirect transfer of heat between
  • At least two e.g. in countercurrent flow such as a warm compressed air stream and one or more cold streams or a cryogenic liquid air product and one or more hot streams.
  • Heat exchangers may be formed from a single or multiple heat exchanger sections connected in parallel and / or in series, e.g. from one or more plate heat exchanger blocks.
  • a heat exchanger for example, the used in an air separation plant "main heat exchanger", thereby
  • pressure level and "temperature level”, causing the It should be stated that appropriate pressures and temperatures in a corresponding plant need not be used in the form of exact pressure or temperature values in order to realize the inventive concept. However, such pressures and temperatures typically range in certain ranges, such as ⁇ 1%, 5%, 10%, 20%, or even 50%
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include unavoidable or expected pressure drops, for example, due to cooling effects.
  • temperature levels include unavoidable or expected pressure drops, for example, due to cooling effects.
  • the inventive method uses an air separation plant with a main air compressor, a main heat exchanger and a distillation column system with a operated at a first pressure level low pressure column and operated at a second pressure level high pressure column.
  • a feed air stream which comprises the entire feed air supplied to the air separation plant, is compressed in the main air compressor to a third pressure level, which is at least 2 bar, in particular
  • the third pressure level may for example also be twice the second pressure level.
  • a first portion is cooled at least once in the main heat exchanger and expanded in a first expansion turbine, starting from the third pressure level.
  • cooled at least once is understood here and below that a corresponding stream before and / or after the relaxation at least once at least through a section of
  • a second portion is treated similarly, ie also cooled at least once in the main heat exchanger and starting in a second expansion turbine relaxed from the third pressure level.
  • the second part is the so-called turbine flow, its relaxation takes place in order to provide additional cooling in a corresponding system and to be able to regulate this.
  • a third portion is further compressed to a fourth pressure level and then also cooled at least once in the main heat exchanger and expanded from the fourth pressure level.
  • the third portion is the so-called inductor current, which, as explained above, in particular the
  • Air of the first portion and / or the second portion and / or the third portion is then at the first and / or at the second pressure level in the
  • the entire air of the first portion is fed to the second pressure level in the high-pressure column.
  • the whole or part of the air of the second share may be on the first
  • Pressure level are fed into the low pressure column and / or at the second pressure level in the high pressure column. The same applies to the third share.
  • the present invention is based on the finding that a combination of a HAP method combined with the energy efficiency of a MAC / BAC
  • Dichtfluidexpander achievable energy saving is coupled to the occurring at the Dichtfluidexpander pressure difference. At lower inlet pressures and thus lower pressure differences, the use is less rewarding overall. Also, improved by the increased pressures of a MAC / BAC process Q, T-profiles can not be conventionally achieved by a HAP method.
  • the final pressure of the main air compressor (in this case the "third pressure level") is determined both by the internal compression pressures, ie the pressures of the gaseous air products to be provided by internal compression, and by the amount of liquid air products to be extracted.
  • the first dependence results from the essentially set by the pressure
  • the plant may only have a variation of the
  • Liquid turbine appears advantageous. As mentioned, the use of a
  • the present invention therefore proposes to further densify the third portion successively in a booster compressor, a first turbine booster and a second turbine booster to the fourth pressure level.
  • a booster compressor a first turbine booster and a second turbine booster
  • at least three compression steps are used, two of which are implemented by a respective turbine booster and one by a secondary compressor.
  • a significantly higher fourth pressure level can be achieved.
  • At least the first turbine booster is operated in the warm, so not as
  • the booster is formed in the invention in one stage, two stages or multi-stage.
  • the booster used in the context of the present invention is to a compressor driven by external energy, which is thus not or at least not exclusively driven by relaxation of a previously compressed in the air separation plant itself fluid.
  • the invention makes it possible by the said compression to provide the third portion (throttle flow) at a significantly increased fourth pressure level, which makes the use of a sealing fluid expander energetically meaningful. thats why
  • the third portion may be the second turbine boosters in particular depending on the amount of liquid or the liquid products that are obtained in a corresponding air separation plant and this should be taken on
  • Turbine booster at a temperature level of 0 to 50 ° C and the second turbine booster at a temperature level of -40 to 50 ° C supply.
  • the second turbine booster is therefore not a typical cold compressor, so no "cold” turbine booster.
  • this is the third portion (throttle current) possibly supplied well below the ambient temperature, downstream of the second turbine booster, however, its temperature is above the ambient temperature.
  • cold turbine boosters are less advantageous because the entire available cooling capacity is used to provide these liquid air products.
  • a cold turbine booster inevitably introduces heat into the system since the heat of compression from the compressed stream typically can not be dissipated in an aftercooler, but only in the main heat exchanger, coupled with a corresponding input of heat.
  • Cooling water enables effective heat dissipation in a conventional aftercooler.
  • the compression in this is substantially heat-neutral, since the compression work is compensated here by the aftercooler.
  • the third portion of the first turbine booster at a temperature level of 0 to 50 ° C and the second turbine booster at a temperature level of -140 to -20 ° C.
  • the second turbine booster is in this case a typical cold compressor, so a "cold" turbine booster. This is the third portion (inductor current) supplied below the ambient temperature, downstream of the second turbine booster, its temperature is still (significantly) below the ambient temperature.
  • the temperature of the second turbine booster is in this case a typical cold compressor, so a "cold" turbine booster.
  • Turbine Booster's condensed third portion may be directly downstream of the second
  • Turbine booster for example, at -90 to 20 ° C lie.
  • a cold turbine booster adds heat to the system since the heat of compression from the compressed stream is typically not present in an aftercooler
  • Cooling water is operated, but only in the main heat exchanger itself, combined with a corresponding heat input, is dissipated.
  • a cold turbine booster permits particularly good heating and liquefaction of internal compression products and is suitable for air separation plants for generating large quantities of corresponding gaseous printed products and comparatively small amounts of liquid air products.
  • the use of a second turbine booster operated at the mentioned low inlet temperatures permits removal of a comparatively small amount of up to 3 mol% of the feed air stream in the form of liquid air products, for example liquid oxygen (LOX), liquid nitrogen (LIN) and / or liquid argon (LAR).
  • LOX liquid oxygen
  • LIN liquid nitrogen
  • LAR liquid argon
  • the invention advantageously provides that said turbine boosters each be driven by one of the expansion turbines, for example the first
  • Turbine booster with the first expansion turbine.
  • After-compressor is, however, driven by external energy, so not via associated expansion turbines, each relax the air portions of the feed air stream. For example, it can be advantageous to use the after-compressor
  • At least one compressor stage of the main air compressor and at least one compressor stage of the secondary compressor are arranged, for example, on a common shaft. Even a use of several appropriate measures can be done simultaneously.
  • the third portion is taken from or fed to the main heat exchanger at appropriate temperature levels.
  • additional after-cooling may be provided downstream of the second turbine booster and before being reintroduced into the main heat exchanger. If, however, the second turbine booster operated at the lower temperatures mentioned, this is, as explained, not the case.
  • the cooling in the main heat exchanger after the recompression in the second turbine booster is advantageously carried out by a temperature level that depends on the inlet and outlet temperature of the second turbine booster and a possible aftercooling, ie, for example, 10 to 50 ° C or -90 to 20 ° C to a temperature level of -140 to -180 ° C. It may also be advantageous if the first portion is cooled to a temperature level of 0 to 150 ° C. before being expanded in the first expansion turbine in the main heat exchanger.
  • the first pressure level is 1 to 2 bar and / or the second pressure level is 5 to 6 bar and / or the third
  • Pressure level 8 to 23 bar and / or the fourth pressure level 50 to 70 bar absolute pressure can be achieved in each case still with conventional HAP main air compressors, the fourth, in particular achieved with the aid of said Nachverêtrs pressure level allows the use of a
  • Dense fluid expander The fourth pressure level is at supercritical pressure.
  • the inventive method allows in particular, the
  • At least one liquid air product distillationklalens fluidly pressurized to evaporate in the main heat exchanger or in the supercritical state (to "liquefy") and run as at least one internal compression product from the air separation plant, so as mentioned several times for use with a internal compression process.
  • the at least one internal compression product can be carried out at a pressure of 6 bar to 100 bar from the air separation plant.
  • the invention Method is due to the additional, above-mentioned heat input in particular for providing internal compression products at a relatively high pressure, ie at least 30 bar, when the second turbine booster is operated at the mentioned lower temperatures.
  • FIG. 1 shows an air separation plant according to an embodiment of the invention in the form of a schematic plant diagram.
  • Figure 2 shows an air separation plant according to an embodiment of the invention in the form of a schematic plant diagram.
  • FIG. 1 shows an air separation plant according to a particularly preferred embodiment
  • Embodiment of the invention shown schematically and designated 100 in total.
  • the air separation plant 100 is used air (AIR) in the form of a
  • the main air compressor 2 is illustrated very schematically.
  • the main air compressor 2 typically has several
  • Compressor stages that have a common shaft with one or more
  • Electric motors can be driven.
  • the third pressure level in the illustrated example is well above the operating pressure of a typical high-pressure column of an air separation plant, as explained above. This is a HAP procedure.
  • the feed air stream b is successively divided into the streams c, d and e.
  • the current c is referred to as the first portion, the current d as the second portion, and the current e as the third portion of the feed air flow b.
  • the streams c and d are separated warm side one
  • the stream c is after removal from the main heat exchanger 4 in an expansion turbine 5, which is referred to in the context of this application as the first expansion turbine to a pressure level of for example 5 to 6 bar, which is referred to in the context of this application as a second pressure level, relaxed, and again passed through a section of the main heat exchanger 4.
  • the stream d is also released to the second pressure level after removal from the main heat exchanger 4 in an expansion turbine 6, which is referred to in the context of this application as a second expansion turbine.
  • the current e is the so-called inductor current, which in particular enables internal compression.
  • the current e is this in a first
  • Expansion turbine 6 powered turbine boosters will be the first here
  • Turbine booster however, referred to as the second turbine booster.
  • the recompression takes place at a pressure level of, for example 50 to 70 bar, which is referred to in this application as the fourth pressure level.
  • Downstream of the booster 7 and upstream of the turbine booster the current e is at a pressure level of for example 26 to 36 bar.
  • the booster 7 is with external energy, ie not by a relaxation of compressed
  • Air fractions of the feed air stream b driven.
  • the current e is recooled in each case in non-separately designated aftercoolers of the turbine boosters to a temperature which corresponds approximately to the cooling water temperature. A further cooling takes place as shown by means of the main heat exchanger 4 as needed.
  • the current e is thus again passed through an aftercooler and then through the main heat exchanger 4 and then expanded in a sealing fluid expander 8.
  • the fourth pressure level is well above the critical pressure for nitrogen and above the critical pressure for oxygen.
  • Dichtfluidexpanders 8 is the current e in the liquid state at
  • the sealing fluid expander 8 is coupled, for example, with a generator or an oil brake (without designation). After relaxation, the current e is here at the second pressure level. He is still liquid, but is at a subcritical pressure.
  • the distillation column system 10 is shown greatly simplified. It comprises at least one at a pressure level of 1 to 2 bar (referred to here as the first pressure level) operated low pressure column 11 and operated at the second pressure level high pressure column 12 of a double column system in which the low pressure column 11 and the high pressure column 12 via a main condenser 13 in heat exchanging connection stand.
  • the first pressure level a pressure level of 1 to 2 bar
  • the second pressure level high pressure column 12 of a double column system in which the low pressure column 11 and the high pressure column 12 via a main condenser 13 in heat exchanging connection stand.
  • valves, pumps, other heat exchangers and the like has been omitted for clarity.
  • the streams c, d and e are fed into the high pressure column 12 in the example shown. However, it may also be provided, for example, the stream d and / or the stream e is not fed into the distillation column system after appropriate expansion into the low-pressure column 1 1 and / or fractions.
  • the distillation column system 10 the currents f, g and h can be removed in the example shown.
  • the air separation plant 100 is set up to carry out an internal compression process, as explained in more detail.
  • the flows f and g which are a liquid,
  • Oxygen-rich stream f and a liquid, nitrogen-rich stream g can act, therefore pressurized by means of pumps 9 in the liquid state and in the
  • Main heat exchanger 4 evaporates or, depending on the pressure, transferred from the liquid to the supercritical state.
  • Fluid of the streams f and g may be the
  • Air separation plant 100 as internally compressed oxygen (GOX-IC) or
  • FIG. 10 illustrates one or more streams taken from the distillation column system 10 in the gaseous state at the first pressure level.
  • FIG. 2 shows an air separation plant according to a particularly preferred embodiment
  • Embodiment of the invention shown schematically and generally designated 200.
  • the same or comparable plant components and streams as in the air separation plant 100 shown in Figure 1 are given identical reference numerals and will not be explained repeatedly.
  • the feed air stream b is also present downstream of the cleaning device 3 at a third pressure level, which, however, here is for example 9 to 17 bar.
  • the fourth pressure level, to which the current e (inductor current) is compressed, is for example 30 to 80 bar here. While the stream e here after the
  • Cooling water temperature corresponds, cooling takes place downstream of the second
  • Turbine Boosters only by means of the main heat exchanger 4, but not by means of an aftercooler as in the air separation plant 100 of Figure 1. Since the second turbine booster is operated as a "cold" turbine booster, the current e downstream of this second turbine booster at a correspondingly low temperature level is well below the ambient temperature in front. In the example shown, the air separation plant 100, the drive of the booster 7 is carried out together with one or more compressor stages of the
  • a pressurized fluid e.g. Compressed steam
  • an air separation plant 100 according to FIG. 1, in which the second turbine booster is operated as a "warm” turbine booster, is particularly suitable for providing larger quantities of liquid air products (not shown), whereas an air separation plant 200 according to FIG.
  • Turbine booster is operated as a "cold" turbine booster, especially for the provision of high pressure gaseous internal compression products.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

L'invention concerne un procédé de séparation cryogénique de l'air dans une installation de séparation d'air (100) comprenant un compresseur d'air principal (2), un échangeur de chaleur principal (4) et un système de colonne de distillation (10) pourvu d'une colonne basse pression (11) fonctionnant à un premier niveau de pression et d'une colonne haute pression (12) fonctionnant à un deuxième niveau de pression, procédé dans lequel un flux d'air d'alimentation (A), qui comporte tout l'air d'alimentation amené à l'installation de séparation d'air (100, 200), est comprimé dans le compresseur d'air principal (2) à un troisième niveau de pression qui est à au moins 2 bar au-dessus du deuxième niveau de pression, le flux d'air d'alimentation comprimé (b) comportant une première partie (c) qui est refroidi au moins une fois dans l'échangeur de chaleur principal (4) et détendu depuis le troisième niveau de pression dans une première turbine de détente (5), une deuxième partie (d) qui est refroidi au moins une fois dans l'échangeur de chaleur principal (4) et détendu depuis le troisième niveau de pression dans une seconde turbine de détente (6), et une troisième partie (e) qui est en outre comprimé à un quatrième niveau de pression, refroidi au moins une fois dans l'échangeur de chaleur principal (4) et détendu depuis le quatrième niveau de pression, l'air de la première partie (c) et/ou de la deuxième partie (d) et/ou de la troisième partie (e) étant introduit au premier et/ou deuxième niveau de pression dans le système de colonne de distillation (10). Selon l'invention, la troisième partie (e) est encore comprimé à un quatrième niveau de pression successivement dans un compresseur secondaire (7), un premier amplificateur de turbine chaud et un deuxième amplificateur de turbine et, pour détendre la troisième partie (e), on utilise un détendeur de fluide d'étanchéité (8) auquel la troisième partie (e) est amenée dans un état liquide et au quatrième niveau de pression. L'invention concerne également une installation de séparation d'air (100).
EP15742185.0A 2014-07-31 2015-07-28 Procédé de séparation cryogénique de l'air et installation de séparation d'air Active EP3175192B1 (fr)

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EP14002683.2A EP2980514A1 (fr) 2014-07-31 2014-07-31 Procédé de séparation cryogénique de l'air et installation de séparation d'air
PCT/EP2015/001554 WO2016015860A1 (fr) 2014-07-31 2015-07-28 Procédé de séparation cryogénique de l'air et installation de séparation d'air

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EP3312533A1 (fr) 2016-10-18 2018-04-25 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
DE102017010001A1 (de) 2016-11-04 2018-05-09 Linde Aktiengesellschaft Verfahren und Anlage zur Tieftemperaturzerlegung von Luft
DE102016015292A1 (de) 2016-12-22 2018-06-28 Linde Aktiengesellschaft Verfahren zur Bereitstellung eines oder mehrerer Luftprodukte mit einer Luftzerlegungsanlage
EP3343158A1 (fr) 2016-12-28 2018-07-04 Linde Aktiengesellschaft Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air
WO2018219501A1 (fr) 2017-05-31 2018-12-06 Linde Aktiengesellschaft Procédé pour produire un ou plusieurs produits formés à partir d'air et installation de séparation d'air
EP3410050B1 (fr) * 2017-06-02 2019-05-01 Linde Aktiengesellschaft Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air
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
EP3620739A1 (fr) 2018-09-05 2020-03-11 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air
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EP3175192C0 (fr) 2024-10-02
CN106716033A (zh) 2017-05-24
EP3175192B1 (fr) 2024-10-02
EP2980514A1 (fr) 2016-02-03
SA517380791B1 (ar) 2020-12-16
WO2016015860A1 (fr) 2016-02-04
CN106716033B (zh) 2020-03-31
US20170234614A1 (en) 2017-08-17

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