EP4065910A1 - Procédé et installation pour fractionnement à basse température de l'air - Google Patents

Procédé et installation pour fractionnement à basse température de l'air

Info

Publication number
EP4065910A1
EP4065910A1 EP20812225.9A EP20812225A EP4065910A1 EP 4065910 A1 EP4065910 A1 EP 4065910A1 EP 20812225 A EP20812225 A EP 20812225A EP 4065910 A1 EP4065910 A1 EP 4065910A1
Authority
EP
European Patent Office
Prior art keywords
rectification column
evaporation
condenser evaporator
condenser
evaporator
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.)
Withdrawn
Application number
EP20812225.9A
Other languages
German (de)
English (en)
Inventor
Stefan Lochner
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 EP4065910A1 publication Critical patent/EP4065910A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure 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
    • F25J3/04048—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
    • 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
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • F25J3/0423—Subcooling of liquid process streams
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—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
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • 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
    • F25J3/04321—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 oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • 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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
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    • F25J2210/42—Nitrogen
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    • 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
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/58—Argon
    • 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
    • F25J2215/60—Methane
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude 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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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 low-temperature decomposition of air and a corresponding system according to the preambles of the independent claims.
  • Air separation plants have rectification column systems which can conventionally be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three- or multi-column systems.
  • rectification columns for obtaining nitrogen and / or oxygen in liquid and / or gaseous state, i.e. the rectification columns for nitrogen-oxygen separation
  • rectification columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • the terms “rectification” and “distillation” as well as “column” and “column” or terms composed of these are often used synonymously.
  • the rectification columns of the rectification column systems mentioned are operated at different pressure levels.
  • Known double column systems have what is known as a high pressure column (also referred to as a pressure column, medium pressure column or lower column) and a so-called low pressure column (also referred to as an upper column).
  • the high pressure column is typically operated at a pressure level of 4 to 7 bar, in particular about 5.3 bar.
  • the low-pressure column is operated at a pressure level of typically 1 to 2 bar, in particular about 1.4 bar. In certain cases, higher pressure levels can also be used in both rectification columns.
  • the pressures specified below are absolute pressures at the top of the columns specified in each case.
  • SPECTRA processes are known from the prior art for providing pressurized nitrogen as the main product. These are explained in detail below.
  • a so-called oxygen column can be used to obtain pure or high-purity oxygen, which can be operated at or above the pressure level of a typical low-pressure column. This is present in addition to the rectification column used for nitrogen production and is fed from this.
  • feed air is cooled in a main heat exchanger and introduced into a single column for nitrogen recovery.
  • a nitrogen product stream is withdrawn from the top of the single column.
  • a first residual fraction is taken from the lower or middle area of the single column, recompressed and then fed back to the single column.
  • An oxygen-containing stream is removed from the individual column at an intermediate point and fed to a pure oxygen column.
  • a pure oxygen product stream is withdrawn in the liquid state from the lower region of the pure oxygen column. The pure oxygen product stream is evaporated and warmed up against feed air in the main heat exchanger and finally obtained as a gaseous product.
  • US Pat. No. 6,279,345 B1 relates to an air separation system that can be used to produce ultra high purity nitrogen or ultra high purity oxygen, with oxygen-enriched liquid from a rectification column being evaporated in two steps using a split top condenser and vapor from the first step being compressed and returned to the rectification column.
  • the object of the present invention is to improve a SPECTRA process with corresponding oxygen production, primarily with regard to energy consumption and material yield. Disclosure of the invention
  • the present invention proposes a method for the low-temperature decomposition of air and a corresponding system with the features of the independent claims.
  • Preferred configurations are the subject matter of the subclaims and the description below.
  • Liquids and gases can be rich or poor in one or more components in the parlance used here, with “rich” for a content of at least 75%, 90%, 95%, 99%, 99.5%, 99.9% or 99.99% and “poor” can mean a content of no more than 25%, 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis.
  • the term “predominantly” can match the definition of "rich”.
  • Liquids and gases can also be enriched or depleted in one or more components, these terms referring to a content in a starting liquid or a starting gas from which the liquid or the gas was obtained.
  • the liquid or the gas is "enriched” if this or this is at least 1, 1 times, 1, 5 times, 2 times, 5 times, 10 times 100 times or 1,000 times the content, and " depleted "if this or this contains at most 0.9 times, 0, 5 times, 0.1 times, 0.01 times or 0.001 times the content of a corresponding component, based on the starting liquid or the starting gas . If, for example, “oxygen”, “nitrogen” or “argon” is used here, this also includes a liquid or a gas that is rich in oxygen or nitrogen, but does not have to consist exclusively of these.
  • pressure level and "temperature level” to characterize pressures and temperatures, which is intended to express that corresponding pressures and temperatures in a corresponding system do not have to be used in the form of exact pressure or temperature values to realize the inventive concept.
  • pressures and temperatures typically move in certain ranges, for example ⁇ 1%, 5% or 10% around a mean value.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include, for example, unavoidable or expected pressure losses.
  • the pressure levels specified here in bar are absolute pressures.
  • expansion machines are typically understood to mean known turboexpander. These expansion machines can in particular also be coupled to compressors. These compressors can in particular be turbo compressors.
  • a corresponding combination of turbo expander and turbo compressor is typically also referred to as a "turbine booster".
  • turbine booster the turbo expander and the turbo compressor 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 a suitable step-up gear).
  • compressor is used here.
  • a “cold compressor” here denotes a compressor to which a fluid flow is fed at a temperature level well below 0 ° C, in particular below -50, -75 or -100 ° C and down to -150 or -200 ° C.
  • a corresponding fluid flow is cooled to a corresponding temperature level in particular by means of a main heat exchanger (see below).
  • a “main air compressor” is characterized by the fact that it compresses all of the air that is fed to the air separation plant and broken down there.
  • further compressors for example booster compressors
  • only a portion of this air that has already been previously compressed in the main air compressor is further compressed.
  • the "main heat exchanger" of an air separation plant represents the heat exchanger in which at least the the majority of the air supplied to the air separation plant and separated there is cooled. This takes place at least in part and possibly only in countercurrent to material flows that are discharged from the air separation plant. Material flows or "products""diverted” from an air separation plant are, in the language used here, fluids that no longer participate in the plant-internal circuits, but are permanently withdrawn from them.
  • a “heat exchanger” for use in the context of the present invention can be designed in a manner customary in the art. It is used for the indirect transfer of heat between at least two fluid flows, for example, which flow in countercurrent to each other, for example a warm compressed air flow and one or more cold fluid flows or a cryogenic liquid air product and one or more warm or warmer, but possibly also cryogenic fluid flows.
  • a heat exchanger can be formed from a single or several parallel and / or serially connected heat exchanger sections, e.g. from one or more plate heat exchanger blocks. It is, for example, a plate heat exchanger (Plate Fin Heat Exchanger).
  • Such a heat exchanger has “passages” which are designed as separate fluid channels with heat exchange surfaces and which are connected to form “groups of passages” in parallel and separated by other passages.
  • a heat exchanger is characterized by the fact that heat is exchanged between two mobile media in it at one point in time, namely at least one fluid flow to be cooled and at least one fluid flow to be heated.
  • a “condenser evaporator” is a heat exchanger in which a condensing fluid flow enters into indirect heat exchange with an evaporating fluid flow.
  • Each condenser-evaporator has a liquefaction space and an evaporation space.
  • the liquefaction and evaporation space have liquefaction and evaporation passages.
  • the condensation (liquefaction) of the condensing fluid stream is carried out in the liquefaction space, and the evaporation of the vaporizing fluid stream in the evaporation space.
  • the evaporation and liquefaction spaces are formed by groups of passages which are in a heat exchange relationship with one another.
  • the present invention comprises the low-temperature decomposition of air according to the so-called SPECTRA method, as is described, inter alia, in EP 2 789 958 A1 and the other patent literature cited therein. In the simplest embodiment, this is a single-column process. However, this is not the case within the scope of the present invention because here, in addition to an air-fed rectification column ("first" rectification column), a rectification column fed from the first rectification column and used to obtain oxygen (“second" rectification column) is used.
  • the SPECTRA process cools compressed and pre-cleaned air to a temperature suitable for rectification. This can partially liquefy it.
  • the air is rectified under the typical pressure of a high pressure column, as explained at the beginning, while obtaining the top gas which is enriched in nitrogen compared to atmospheric air and a liquid bottom liquid which is enriched in oxygen compared to atmospheric air.
  • a reflux of the first rectification column used for this purpose is provided by condensing overhead gas from the first rectification column, more precisely part of this overhead gas, in a heat exchanger.
  • a condenser evaporator (“first" condenser evaporator), fluid, which is also taken from the first rectification column, is used for cooling and is evaporated or partially evaporated in the process.
  • Additional overhead gas can be provided as a nitrogen-rich product.
  • first and second streams are used in the first condenser-evaporator, the first stream being formed using liquid that is taken from the first rectification column with a first oxygen content , and the second stream is formed using liquid which is withdrawn from the first rectification column with a second, higher oxygen content.
  • the liquid used to form the first stream can be withdrawn from the first rectification column from an intermediate tray or from a liquid retention device.
  • the liquid used to form the second stream can in particular be at least part of the liquid bottom product of the first rectification column.
  • the first and second streams are the fluid mentioned, which is used in the first condenser-evaporator for cooling and for condensing the corresponding portion of top gas of the first rectification column.
  • the first stream can be at least partially compressed by means of a cold compressor and returned to the first rectification column.
  • the second material flow can be at least partially expanded and implemented as a so-called residual gas mixture from the air separation plant.
  • one or more compressors can be used, which is or are coupled to one or more expansion machines in which the expansion of the second material flow (or a corresponding one) Partly) is made.
  • a compressor can be used here which is coupled to one of two expansion machines arranged in parallel. If only one expansion machine is used, the compressor can be coupled to it.
  • the compressor or compressors described does not have to or do not have to be driven, in particular not exclusively, by means of the one or more mentioned expansion machines. Conversely, the compressor or compressors do not have to take up all of the work released during the expansion.
  • a supporting or exclusive drive can also take place using an electric motor, or a brake can be interposed between the expansion machine (s) and the compressor (s).
  • the compressor or compressors are one or more cold compressors, since the first fluid flow is fed to this or them despite being guided through the first condenser evaporator and possibly subsequent further heating at a low temperature level.
  • second condenser evaporator in the lower region of the second rectification column, which is used to boil bottom liquid from the second rectification column.
  • This is conventionally operated with (at least) air (feed air) compressed in the main air compressor and cooled in the main heat exchanger, which is fed to the first rectification column.
  • this can also be air which is initially in gaseous form and which is liquefied in the second condenser-evaporator before it is fed into the first rectification column. It is part of the total feed air fed to the first rectification column. Further (gaseous) feed air can be fed into the first rectification column without a corresponding liquefaction.
  • This (liquefied) partial air flow is then used (after its evaporation) to generate cooling capacity or to drive the cold compressor (s) used by taking a corresponding amount of fluid as a second material flow from the first rectification column, but no longer takes part in the rectification process the first rectification column part.
  • the high driving temperature difference in the second condenser evaporator in the lower area of the second rectification column leads to additional thermodynamic losses in the process.
  • these disadvantages have a strong effect on the power consumption of the main air compressor.
  • the present invention is based on the knowledge that a method of the type explained above can be modified particularly advantageously in that instead of a feed air stream in the second condenser evaporator in the lower region of the second rectification column, fluid is used which, in the manner explained above, is part of the " first "or" second "stream was evaporated in the first condenser evaporator. In this way, the air previously used for this purpose can be saved, thereby increasing energy efficiency and yield.
  • the condensed fluid can then be treated as explained below.
  • the invention also develops particular advantages in that the condensation in the second condenser evaporator is carried out at a pressure level at which the corresponding fluid was previously evaporated in the first condenser evaporator. In this way, a renewed compression can be dispensed with and the condensed gas or the condensate formed can be brought to the required pressure by means of a pump become. In contrast to a gas compressor, the operation of a pump is significantly more reliable and its provision is significantly more cost-effective.
  • the present invention proposes, in the parlance of the patent claims, a method for the low-temperature separation of air in which an air separation plant with a first rectification column and a second rectification column is used.
  • the first rectification column is operated at a first pressure level and the second rectification column is operated at a second pressure level below the first pressure level.
  • first and second pressure levels are typical pressure levels as are also used in conventional air separation plants, in particular SPECTRA plants with oxygen production.
  • the first pressure level can in particular be 7 to 14 bar, the second pressure level in particular 1, 2 to 5 bar.
  • the second pressure level can generally also be 1 to 4 bar.
  • These are absolute pressures at the top of the respective rectification columns.
  • the first rectification column and the second rectification column can in particular be arranged next to one another and are typically not combined with one another in the form of a double column, a "double column” being understood here generally to mean a separation apparatus formed from two rectification columns, which is designed as a structural unit with column jackets of the two rectification columns are connected to one another without a line, ie directly, in particular by welding. However, this direct connection alone does not have to produce a fluidic connection.
  • the first rectification column used in the context of the present invention and the second rectification column used in the context of the present invention have already been described in detail above with reference to the SPECTRA process.
  • the second rectification column can in particular be an oxygen column.
  • the first rectification column is supplied with atmospheric air, which has been compressed and then cooled. If appropriate, appropriate air can be fed to the first rectification column in the form of several streams which are treated differently and, if necessary, previously passed through further apparatus can. In contrast, typically no air is fed to the second rectification column.
  • the second rectification column is fed from the first rectification column or the second rectification column is typically not fed any streams that were not previously removed from the first rectification column or were not formed from such streams.
  • top gas from the first rectification column is obtained as a nitrogen product and discharged from the air separation unit
  • bottom liquid from the second rectification column is obtained as an oxygen product and discharged from the air separation unit.
  • further fluids for example top gas of the second rectification column
  • Fluids that are otherwise discharged as nitrogen or oxygen products can also be discharged in certain parts within the scope of the present invention, for example as purge streams or another liquid nitrogen product after condensation of top gas from the first rectification column.
  • first and a second stream of material are subjected to evaporation separately from one another below the first pressure level.
  • the evaporation pressures in the first condenser evaporator are in particular 3.5 to 7.5 bara (bar absolute pressure, the values can represent exact or approximate values) depending on the first pressure level. Therefore, the fluid to be evaporated here, which was taken from the first rectification column, is correspondingly expanded. Further top gas of the first rectification column, which is not provided as a gaseous nitrogen product, is condensed in the first condenser-evaporator and returned as reflux to the first rectification column. A proportion of the corresponding condensate can also be discharged as the mentioned further liquid nitrogen product, in particular after being supercooled against itself.
  • the first stream evaporated in the first condenser-evaporator is in the context of the present invention using liquid that is taken from the first rectification column with a first oxygen content, and the The second stream is formed using liquid which is withdrawn from the first rectification column with a second oxygen content above the first oxygen content. Further information on such liquids has already been explained.
  • the liquid with the first, lower oxygen content is, in particular, liquid that is obtained on an intermediate tray or separating tray of the first rectification column or a corresponding liquid retention device.
  • the liquid with the second, higher oxygen content is in particular the bottom liquid of the first rectification column.
  • gas from the first stream after its evaporation or partial evaporation in the first condenser evaporator, is partially or completely subjected to a recompression to the first pressure level and fed into the first rectification column, and gas from the second stream is after its evaporation or partial evaporation in the first Condenser evaporator subjected to relaxation and discharged from the air separation plant.
  • gas of the first material flow and “gas of the second material flow” should in particular also encompass the fact that the entire gas of the first or second material flow is used in the manner explained, if not a certain part in embodiments of the present invention is used in a different way, as explained below.
  • gas of the first stream and “gas of the second stream” is intended to denote, in other words, all or part of the corresponding gas, but does not exclude the fact that other uses may also be present within the scope of the invention.
  • the second rectification column is equipped with or at least thermally coupled to the second condenser evaporator, the second condenser evaporator being designed or provided in particular in a sump area of the second rectification column and in particular partially submerged in a liquid bath forming in the sump area.
  • the bottom liquid of the second rectification column is evaporated in the second condenser-evaporator.
  • liquid can also be cooled (subcooled) by means of which the second rectification column is fed from the first rectification column.
  • gas of the first or second stream after its evaporation or partial evaporation in the first condenser evaporator, is subjected to condensation in the second condenser evaporator and, in particular after a corresponding pressure increase in the liquid state, at least in part to the liquid that the first rectification column with the first or the second oxygen content is withdrawn and used in the formation of the first or second stream, fed in, or instead fed into a lower region of the first rectification column.
  • gas from the first or second stream other gas from the first or second stream or the respective unaffected stream is used partially or completely in the manner explained (recompressed and returned to or returned to the first rectification column). relaxed and diverted).
  • the two alternatives of the invention are in particular that a first portion of the first material flow is subjected to recompression to the first pressure level after its evaporation in the first condenser evaporator, and that a second portion of the first material flow after it Evaporation in the first condenser evaporator Condensation in the second condenser evaporator is subjected, on the one hand, or that a first portion of the second material flow after its evaporation in the first condenser evaporator is subjected to the work-performing expansion, and that a second portion of the second material flow after its evaporation in the first condenser evaporator Is subjected to condensation in the second condenser-evaporator, on the other hand.
  • the gas of the first or second material flow which after evaporation or partial evaporation in the first condenser evaporator is subjected to condensation in the second condenser evaporator, is subjected to condensation in the second condenser evaporator at a pressure level at which it has previously been subjected to evaporation or partial evaporation in the first condenser evaporator.
  • the gas of the first or second material flow which after evaporation or partial evaporation in the first condenser evaporator is subjected to condensation in the second condenser evaporator, in particular using a gas line that couples the first condenser evaporator and the second condenser evaporator without a compressor, is fed into the second condenser evaporator convicted.
  • a direct coupling implemented without pressure-influencing devices can be provided here.
  • At least part of a condensate formed during condensation in the first condenser evaporator is subjected to a pressure increase in the liquid state using a pump.
  • the pressure increase in the liquid state is carried out in particular to the first pressure level.
  • At least part of the condensate formed during the condensation in the first condenser-evaporator and subjected to the pressure increase in the liquid state can be used in the above-mentioned first alternative to the liquid that is taken from the first rectification column with the first or second oxygen content and during the formation of the first or second stream is used, or, in the other alternative also mentioned, are fed into a lower region of the first rectification column.
  • gas of the first or second material flow can be subjected to condensation in the second condenser evaporator after its evaporation or partial evaporation in the first condenser evaporator and, after a corresponding pressure increase in the liquid state, at least partially are fed into a lower region of the first rectification column.
  • a “lower region” can advantageously be a position at which the first stream of material evaporated in the first condenser-evaporator or its liquid is withdrawn from the first rectification column.
  • the pressurized nitrogen product from the first rectification column could also be used to heat the second condenser evaporator and subjected to a corresponding condensation.
  • a correspondingly contamination-free working pump would have to be used to convey the liquid formed further. Because of the expense involved, this is extremely disadvantageous compared to the solutions proposed according to the invention.
  • one or more compressors can also be provided within the scope of the present invention for the recompression of the gas of the first stream after its evaporation or partial evaporation in the first condenser evaporator, and for the expansion of the gas in the second Material flow after its evaporation or partial evaporation in the first condenser-evaporator can be provided one or more expansion machines which is or are coupled to the one or more compressors. Further details have already been explained above for the SPECTRA method in general.
  • an overhead gas of the first rectification column and thus a nitrogen product, with a content of less than 1 ppb oxygen, carbon monoxide and / or hydrogen and a content of less than 10 ppm argon on a volume basis, can be obtained.
  • the bottom liquid of the second rectification column can have a content of less as 10 ppb argon and / or 5 ppm methane on a volume basis and otherwise consists essentially of oxygen.
  • the first rectification column can be operated in such a way that the first pressure level is 7 to 14 bar absolute pressure, in particular 8 to 12 bar, and that the second pressure level is 1, 2 to 5 bar, in particular 2 to 4 bar, absolute pressure.
  • all of the cooled compressed air to be separated in the process is fed in gaseous form into the first rectification column.
  • the present invention also extends to an air separation plant which has a first rectification column, a second rectification column, a first condenser evaporator and a second condenser evaporator and is set up to feed the first rectification column with air and operate it at a first pressure level and the second rectification column to feed from the first rectification column and operate at a second pressure level below the first pressure level.
  • the air separation plant is also set up to obtain top gas from the first rectification column as a nitrogen product and to discharge it from the air separation unit and to obtain bottom liquid from the second rectification column as an oxygen product and to discharge it from the air separation unit
  • means are provided which are set up to subject gas of the first or second stream after its evaporation or partial evaporation in the first condenser evaporator to condensation in the second condenser evaporator and at least in part to the liquid that the first rectification column with withdrawn from the second oxygen content and used in the formation of the second stream, feed or feed into a lower region of the second rectification column.
  • one or more compressors are required and for the expansion of the gas of the second material flow after its evaporation or partial evaporation in the first condenser evaporator one or more, with one or more Compressors mechanically coupled expansion machines provided.
  • the first condenser evaporator and the second condenser evaporator are arranged and, in particular, coupled to one another via a gas line without a compressor, that the gas of the first or second material flow that is subjected to condensation in the second condenser evaporator after evaporation or partial evaporation in the first condenser evaporator is condensed in the second condenser evaporator is subjected to a pressure level at which it was previously subjected to evaporation or partial evaporation in the first condenser evaporator.
  • Figure 1 shows an air separation plant according to an embodiment of the invention.
  • Figure 2 shows an air separation plant according to an embodiment of the invention.
  • FIG. 3 shows an air separation plant according to an embodiment of the invention.
  • an air separation plant 100 is illustrated in the form of a schematic plant diagram.
  • the central component is a distillation column system with a first rectification column 11, a second rectification column 12, a first condenser evaporator 111 and a second condenser evaporator 121.
  • the first rectification column 11 is operated at a first pressure level and the second rectification column 12 is operated at a second pressure level below the first pressure level operated.
  • a main air compressor 1 of the air separation plant 100 By means of a main air compressor 1 of the air separation plant 100, air is sucked in and compressed from the atmosphere A via a filter which is not specifically designated. After cooling in an aftercooler, also not specifically designated, downstream of the main air compressor 1, the feed air flow a formed in this way is further cooled in a direct contact cooler 2 operated with water W. The feed air flow a is then subjected to cleaning in an adsorber unit 3.
  • the feed air stream a is fed into the first rectification column 11.
  • part of the feed air stream a would be fed into the first rectification column 11, while a further part would be fed through the second condenser evaporator 121, which is in a lower Area of the second rectification column 12 is arranged, and by means of the bottom liquid of the second rectification column 12 is evaporated.
  • This further part would be condensed in the second condenser-evaporator 121 and then likewise fed into the first rectification column 11. As mentioned, this is not the case in the embodiments of the invention.
  • Top gas of the first rectification column 11 is discharged from the air separation plant 300 in the form of a stream d as nitrogen product B or sealing gas C.
  • Bottom liquid from the second rectification column 12, on the other hand, is discharged as an oxygen product D in the form of a stream e.
  • it can also be fed into so-called run tanks for later evaporation to provide an internally compressed oxygen product D.
  • a first material flow g and a second material flow h below the first pressure level are subjected to evaporation.
  • Further top gas from the first rectification column 11 is condensed in the form of a stream i in the first condenser-evaporator 111 and returned as reflux to the first rectification column 11.
  • a part can also, as illustrated here in the form of a material flow k, be supercooled in a subcooler 5 and provided as liquid nitrogen F.
  • a stream I heated in the process is treated as explained in more detail below.
  • a further discharge in the form of a purge flow m or P can also be provided.
  • the first stream g is using liquid that is taken from the first rectification column 11 with a first oxygen content
  • the second stream h is using liquid (in particular bottom liquid) that the first rectification column 11 with a second oxygen content above the first oxygen content is taken, formed.
  • gas from the first stream g is subjected to a recompression to the first pressure level in a compressor 6 and fed into the first rectification column 11.
  • a part illustrated by dashed lines can also be returned for compression in the compressor 6.
  • Part of the material flow g can also be released into the atmosphere A in the form of a material flow n.
  • gas of the second stream h is subjected to a parallel further expansion in expansion machines 7 and 8, combined with top gas, which is withdrawn in the form of a stream o from the second rectification column 12, and after being heated in the Main heat exchanger 4 is used as a regeneration gas in adsorber unit 3 or released to atmosphere A and thus discharged from air separation plant 300.
  • the expansion machine 7 is coupled to the compressor 6, and the expansion machine 8 is coupled to a generator G.
  • a different number of corresponding machines or a different type of coupling can also be used in each case.
  • An (oil) brake that is not specifically designated can also be provided.
  • the second rectification column 12 is fed with a side stream p of the first rectification column 11, which is passed through the second condenser-evaporator 121 and is fed to the second rectification column in an upper region. Furthermore, gas of the second material flow h is passed through the condenser evaporator 121 after its evaporation or partial evaporation in the first condenser evaporator 111 as a partial flow b and is subjected to a condensation. Correspondingly formed liquid, further denoted by b, is increased in pressure by means of a pump 9 and then reunited with the second stream h before its evaporation.
  • the pressure of the liquid formed in the condenser evaporator 121 by condensing gas from the second stream h in the form of the stream b is increased by means of the pump 9, but then into the first rectification column 11 in fed into a lower area.
  • a partial flow of the first material flow g can also be used accordingly, as illustrated in FIG. 3 with a material flow c.
  • the air separation plant 300 according to FIG. 3 can otherwise be designed essentially identically or in a comparable manner.
  • the liquid formed in the second condenser-evaporator 121 by condensing gas from the first material flow g is increased in pressure by means of the pump 9 and then combined again with the first material flow g before evaporation in the first condenser-evaporator 111.

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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)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Abstract

Un procédé SPECTRA est proposé pour le fractionnement à basse température de l'air, dans lequel un liquide de fond provenant d'une seconde colonne de rectification supplémentaire (12) utilisé pour obtenir de l'oxygène est évaporé dans un second condenseur-évaporateur (121). Dans ledit second condenseur-évaporateur (121), du gaz qui a été préalablement évaporé dans un premier condenseur-évaporateur (111), qui est utilisé pour la condensation de gaz de tête provenant d'une première colonne de rectification (11), est condensé au niveau de pression de l'évaporation précédente. XXX L'invention concerne également une installation correspondante (100, 200, 300).
EP20812225.9A 2019-11-26 2020-11-24 Procédé et installation pour fractionnement à basse température de l'air Withdrawn EP4065910A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP19020664 2019-11-26
PCT/EP2020/025532 WO2021104668A1 (fr) 2019-11-26 2020-11-24 Procédé et installation pour fractionnement à basse température de l'air

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EP4065910A1 true EP4065910A1 (fr) 2022-10-05

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US (1) US20220260312A1 (fr)
EP (1) EP4065910A1 (fr)
CN (1) CN113924452A (fr)
IL (1) IL288739B2 (fr)
WO (1) WO2021104668A1 (fr)

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CN117157498A (zh) * 2021-04-09 2023-12-01 林德有限责任公司 用于低温分离空气的方法和设备
JP2024058676A (ja) * 2022-09-06 2024-04-26 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 空気分離装置および空気分離方法

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JP3719832B2 (ja) * 1997-10-14 2005-11-24 日本エア・リキード株式会社 超高純度窒素及び酸素の製造装置
US6279345B1 (en) * 2000-05-18 2001-08-28 Praxair Technology, Inc. Cryogenic air separation system with split kettle recycle
DE102007024168A1 (de) * 2007-05-24 2008-11-27 Linde Ag Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
DE102008064117A1 (de) * 2008-12-19 2009-05-28 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
CN103998883B (zh) * 2011-09-20 2016-12-14 林德股份公司 低温分离空气的方法和设备
EP2789958A1 (fr) 2013-04-10 2014-10-15 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air
JP6900241B2 (ja) * 2017-05-31 2021-07-07 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード ガス製造システム
JP7313608B2 (ja) * 2019-04-08 2023-07-25 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 高純度酸素および窒素製造システム

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IL288739B2 (en) 2023-07-01
IL288739A (en) 2022-02-01
CN113924452A (zh) 2022-01-11
WO2021104668A1 (fr) 2021-06-03
US20220260312A1 (en) 2022-08-18
IL288739B1 (en) 2023-03-01

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