EP1143216B1 - Verfahren und Vorrichtung zur Erzeugung von sauerstoffreicher Flüssigkeit durch kryogenische Luftzerlegung - Google Patents

Verfahren und Vorrichtung zur Erzeugung von sauerstoffreicher Flüssigkeit durch kryogenische Luftzerlegung Download PDF

Info

Publication number
EP1143216B1
EP1143216B1 EP01400749A EP01400749A EP1143216B1 EP 1143216 B1 EP1143216 B1 EP 1143216B1 EP 01400749 A EP01400749 A EP 01400749A EP 01400749 A EP01400749 A EP 01400749A EP 1143216 B1 EP1143216 B1 EP 1143216B1
Authority
EP
European Patent Office
Prior art keywords
column
argon
flow
enriched
oxygen
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.)
Expired - Lifetime
Application number
EP01400749A
Other languages
English (en)
French (fr)
Other versions
EP1143216A1 (de
Inventor
Benoît DAVIDIAN
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.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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 Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP1143216A1 publication Critical patent/EP1143216A1/de
Application granted granted Critical
Publication of EP1143216B1 publication Critical patent/EP1143216B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • F25J3/04248—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
    • 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
    • F25J3/04078—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
    • F25J3/04127—Gas 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
    • 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04575—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for a gas expansion plant, e.g. dilution of the combustion gas in a gas turbine
    • 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • F25J3/046—Completely integrated air feed compression, i.e. common MAC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • 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
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

Definitions

  • the present invention relates to a process and apparatus for producing an oxygen-enriched fluid by cryogenic distillation of a mixture containing nitrogen, oxygen and argon, according to the preambles of claims 1 and 12 respectively and as of document EP-A-0 795 728 .
  • it relates to a method and apparatus for separating air by cryogenic distillation allowing the production of pure oxygen, ie oxygen containing at least 95 mol%. oxygen, preferably at least 98 mol%. of oxygen or even 99.5 mol%. oxygen.
  • the patent application EP-A-0540900 discloses a process for producing impure oxygen in which a portion of the impure argon containing at least 90% argon of a mixture column is mixed with the residual nitrogen of a double column.
  • the mixture column operates at the same low pressure as the low pressure column, up to 1.75 bara.
  • EP-A-0384213 has a low pressure column operating at between 1.5 and 10 bara but the argon column operates at a lower pressure.
  • US Patent 4932212 describes the case in which the low pressure column and the argon column operate at pressures between 1 and 2 bars.
  • EP-A-0518491 discloses a process for producing nitrogen gas under pressure and incidentally liquid nitrogen, liquid argon and liquid oxygen in which the low pressure column and the argon column operate at a substantially identical pressure above 2.5 bara. No flow of argon gas is produced.
  • EP-A-0952415 describes an apparatus comprising a double column and an argon column operating with a yield lower than the optimal yield.
  • An object of the present invention is to increase the pure oxygen yield of an air separation apparatus.
  • Another object of the invention is to provide an air separation apparatus particularly well suited to the demands of large quantities of nitrogen under pressure (typically in the case of integration with a gas turbine of a IGCC).
  • the flow enriched in argon or optionally the flow enriched in argon mixed with a gas enriched in nitrogen is sent upstream of the expansion machine of a gas turbine.
  • the flow enriched with argon may contain between 10 and 95 mol%. argon (or between 40 and 95 mol% of argon), between 2 and 40 mol% of oxygen and between 2 and 40 mol%. nitrogen.
  • argon production for example by withdrawing a flow richer in argon from the auxiliary column which is the product.
  • the argon enriched flow that is sent upstream of the expansion machine of a gas turbine can constitute between 0.3 and 2% of the air, preferably between 0.5 and 1% of the air. For this reason, it is preferable to mix the argon-enriched flow with a nitrogen-enriched gas containing at least 90 mol%. nitrogen from eg the low pressure column of a double column and use the mixture in a gas turbine and currently relax the mixture in a turbine.
  • the mixture formed comprises less than 2 mol%. argon, preferably less than 1 mol%. argon.
  • the low pressure column can operate between 2 and 10 bara, preferably above 2.5 bara.
  • the apparatus may comprise an auxiliary flow separation column containing at least argon and oxygen and two other columns, including a high pressure column and a low pressure column thermally connected to each other, auxiliary column being fed from the low pressure column.
  • the apparatus may comprise an auxiliary flow separation column containing at least argon and oxygen and at least three other columns, including a high pressure column, an intermediate pressure column and a low pressure column connected. thermally between them, the auxiliary column being fed from the low pressure column or the intermediate pressure column.
  • an integrated air separation and energy production method comprising a method according to claim 1, in which a nitrogen-enriched gas is sent from the column preferably operating at the pressure a. lower to the gas turbine, after a possible compression step and optionally sends an oxygen-enriched fluid from a column of the apparatus to a gasifier.
  • the auxiliary column contains between 30 and 40 theoretical plates.
  • the separation of oxygen and argon in the bottom of the low pressure column is facilitated.
  • the fluid enriched with argon withdrawn from the auxiliary column is not necessarily an end product of the apparatus but can be used to cool the flow rates entering the columns or to provide frigories by expansion.
  • an air flow 1 of 1000 Nm 3 / h is purified by adsorbent beds 4 and is divided in two.
  • the flow 2 is supercharged at a higher pressure, sent into the heat exchanger 3 where it cools by vaporizing the liquid oxygen and then to a hydraulic turbine 5 from which it comes out in at least partially liquid form .
  • This liquid (or two-phase mixture) 7 is sent to the high pressure column 9 operating between 14 and 15 bar and possibly partly to the low pressure column 11 operating between 4 and 6 bar (or even between 2 and 10 bar), or sending a portion of the liquid of a capacity upstream of the medium pressure column or by withdrawing a flow rate having a composition similar to that of the liquid air of the high pressure column 9, as shown in FIG. figure 1 .
  • the apparatus may include an insufflation turbine which serves during startup. It comprises a low pressure nitrogen turbine 55.
  • a rich liquid flow 15 is withdrawn from the high pressure column and sent to the subcooler 17, divided in two and sent partly to the low pressure column, after expansion in the valve 21 and in part to the top condenser 23 of the column after the expansion in the valve 27.
  • the rich liquid at least partially vaporized in the overhead condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a gas flow are sent from the condenser to the column. low pressure.
  • a nitrogen gas flow rate 19 may optionally be withdrawn from the top of the high pressure column 9.
  • the auxiliary column is fed with a gas flow 29 containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • the vessel liquid 31 of the auxiliary column is returned to the low pressure column which operates substantially at the same pressure as the auxiliary column.
  • the auxiliary column 25 may alternatively be fed with a liquid flow rate containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • column 25 will have a bottom reboiler heated by a gas flow such as air or nitrogen from the high pressure column 9.
  • a liquid air flow 33 and a low liquid flow rate 35 are sent from the high pressure column 9 to the low pressure column 11, after having been subcooled in the subcooler 17 and expanded in valves.
  • a flow of liquid oxygen 37 containing 99.5 mol%. oxygen is withdrawn in the bottom of the low pressure column, pressurized by a pump 39 and vaporized in the exchanger 3.
  • An argon-enriched gas 49 constituting between 0.5 and 1% of the air supplied to the apparatus and containing between 40 and 95 mol%.
  • Argon withdrawn from the head of the auxiliary column 25 is mixed with residual nitrogen 47 from the head of the low pressure column.
  • the mixture 54 heats up in the subcooler 17 and then warms up in the exchanger 3.
  • the mixture is then sent upstream of the expansion machine 51 of a gas turbine after a compression step.
  • the process of the Figure 1 can increase the oxygen yield from 78% to 90%.
  • a triple column is used instead of the double column of the Figure 1 .
  • An air flow 1 is purified by adsorbent beds 4 and is divided in two.
  • the flow 2 is supercharged at a higher pressure, sent into the heat exchanger 3 where it cools by vaporizing the liquid oxygen and then to a hydraulic turbine 5 from which it comes out in at least partially liquid form .
  • This liquid (or two-phase mixture) 7 is sent to the high pressure column 9 operating between 14 and 15 bar and possibly partly to the low pressure column 11 operating between 4 and 6 bar and / or optionally to the intermediate pressure column 40 operating between 7 and 9 bar, either by sending a portion of the liquid of a capacity upstream of the medium pressure column or by withdrawing a flow rate having a composition similar to that of the liquid air of the high pressure column 9, as shown in FIG. figure 2 .
  • the apparatus may include an insufflation turbine which serves during startup. It comprises a low pressure nitrogen turbine 55.
  • a rich liquid flow 15 is withdrawn from the high pressure column and sent to the subcooler 17, divided in two and sent partly to the middle of the column operating at intermediate pressure 40, after expansion in the valve 21 and partly to the condenser of head 23 of the auxiliary column 25 after expansion in the valve 27.
  • the rich liquid at least partially vaporized in the head condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a gas flow are sent from the condenser to the low pressure column.
  • a nitrogen gas flow rate 19 may optionally be withdrawn from the top of the high pressure column 9.
  • the auxiliary column is fed with a portion of a gas flow 29 containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • the vessel liquid 31 of the auxiliary column is returned to the low pressure column which operates substantially at the same pressure as the auxiliary column.
  • the auxiliary column 25 may alternatively be fed with a liquid flow rate containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • column 25 will have a bottom reboiler heated by a gas flow such as air or nitrogen from the high pressure column 9.
  • the remainder of the gas flow 29 serves to heat the bottom reboiler 41 of the column 40 and after condensation is returned to the low pressure column with the flow 31.
  • the tank liquid 43 of the column 40 is sent partly directly to the low pressure column and partly to the top condenser of the column 40 where it is vaporizes at least partially before being sent to the low pressure column in turn.
  • the overhead liquid 47 of the column 40 is undercooled in the exchanger 17, expanded, mixed with the expanded flow 35 and sent to the top of the low pressure column.
  • a liquid air flow 33 and a low liquid flow rate 35 are sent from the high pressure column 9 to the low pressure column 11, after having been subcooled in the subcooler 17 and expanded in valves.
  • a flow of liquid oxygen 37 containing 99.5 mol%. oxygen is withdrawn in the bottom of the low pressure column, pressurized by a pump 39 and vaporized in the exchanger 3.
  • An argon-enriched gas 49 constituting between 0.5 and 1% of the air supplied to the apparatus and containing between 40 and 95 mol%.
  • Argon withdrawn from the head of the auxiliary column 25 is mixed with residual nitrogen 47 from the head of the low pressure column.
  • the mixture 54 heats up in the subcooler 17 and then warms up in the exchanger 3.
  • the mixture is then sent upstream of the expansion machine 51 of a gas turbine after a possible compression step.
  • the process according to the invention is of particular interest in the case in which the nitrogen of the low pressure column is upgraded, by sending it to an expansion machine 51 of a gas turbine.
  • at least part of the air 1 can come from the compressor 53 of the gas turbine and the oxygen produced by the distillation apparatus can be used for the gasification necessary to produce the fuel of the gas turbine.

Landscapes

  • 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)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)

Claims (14)

  1. Verfahren zur Produktion eines mit Sauerstoff angereicherten Stroms in einer Vorrichtung zur Tieftemperaturdestillation, das die folgenden Schritte umfasst:
    a) Abkühlen eines Versorgungsstroms (1), der Sauerstoff, Stickstoff und Argon enthält, und Einleiten dieses Stroms in eine Destillationsvorrichtung mit einer Hilfskolonne (25) zur Abscheidung eines Stroms (29), der mindestens Argon und Sauerstoff enthält, und mit mindestens zwei anderen Kolonnen (9, 18);
    b) Abscheiden dieses Stroms durch Tieftemperaturdestillation in der Vorrichtung, so dass mit Sauerstoff und Stickstoff angereicherte Fluide gebildet werden (15, 33, 35);
    c) Leiten des Stroms, der mindestens Argon und Sauerstoff enthält, von einer der anderen Kolonnen zu der Hilfskolonne, wobei die Hilfskolonne im Wesentlichen bei demselben Druck arbeitet wie die Kolonne (18), von welcher der Strom stammt, der mindestens Argon und Sauerstoff enthält, wobei dieser Druck zwischen 2 und 10 bar absolut beträgt;
    d) Abziehen eines mit Sauerstoff angereicherten Stroms (37), der mindestens 95 Mol-% Sauerstoff enthält, aus einer Kolonne der Vorrichtung;
    e) Abziehen eines mit Argon angereicherten Stroms (49) aus der Hilfskolonne;
    dadurch gekennzeichnet, dass mindestens ein Teil des mit Argon angereicherten Stroms (49) stromaufwärts der Entspannungsmaschine (51) einer Gasturbine geleitet wird, gegebenenfalls nachdem er mit einem mit Stickstoff angereicherten Gas der Vorrichtung vermischt wurde, und dass ein Gas (54) aus der Kolonne (18), die mit dem niedrigsten Druck arbeitet, außer der Hilfskolonne, abgezogen wird und an eine Entspannungsturbine (55) geleitet wird, ohne zwischen der Kolonne, aus der es abgezogen wurde, und der Entspannungsturbine verdichtet zu werden.
  2. Verfahren nach Anspruch 1, wobei der mit Argon angereicherte Strom (49) zwischen 10 und 95 Mol-% Argon enthält.
  3. Verfahren nach Anspruch 2, wobei der mit Argon angereicherte Strom (49) zwischen 40 und 95 Mol-% Argon enthält.
  4. Verfahren nach Anspruch 1 oder 2, wobei der mit Argon angereicherte Strom (49) zwischen 2 und 40 Mol-% Sauerstoff enthält.
  5. Verfahren nach einem der vorhergehenden Ansprüche, wobei mindestens ein Teil des mit Argon angereicherten Stroms (49) an die Atmosphäre zurückgegeben wird, gegebenenfalls nachdem er mit einem mit Stickstoff angereicherten Gas der Vorrichtung vermischt wurde.
  6. Verfahren nach einem der vorhergehenden Ansprüche, wobei mindestens ein Teil des mit Argon angereicherten Stroms (49) zur Regeneration von Adsorptionsmittelschüttungen (4) oder umschaltbaren Wärmetauschern dient, gegebenenfalls nachdem er mit einem mit Stickstoff angereicherten Gas der Vorrichtung vermischt wurde.
  7. Verfahren nach einem der Ansprüche 1 bis 6, wobei die Produktion eines mit Argon angereicherten Fluids als Endprodukt erfolgt.
  8. Verfahren nach einem der vorhergehenden Ansprüche, wobei mindestens ein Teil des mit Argon angereicherten Stroms (49) zu der Entspannungsturbine (55) oder einem Druckminderventil geleitet wird, gegebenenfalls nachdem er mit einem mit Stickstoff angereicherten gasförmigen Strom vermischt wurde.
  9. Verfahren nach einem der vorhergehenden Ansprüche, wobei die mindestens zwei anderen Kolonnen eine Hochdruckkolonne (9) und eine Niederdruckkolonne (18) umfassen, die thermisch miteinander verbunden sind, und die Hilfskolonne von der Niederdruckkolonne aus versorgt wird.
  10. Verfahren nach einem der Ansprüche 1 bis 8, wobei die Vorrichtung mindestens drei andere Kolonnen umfasst, darunter eine Hochdruckkolonne (9), eine Mitteldruckkolonne (40) und eine Niederdruckkolonne (18), die thermisch miteinander verbunden sind, und die Hilfskolonne von der Niederdruckkolonne oder der Mitteldruckkolonne aus versorgt wird.
  11. Integriertes Verfahren zur Abscheidung von Luft und zur Erzeugung von Energie, umfassend ein Verfahren nach Anspruch 1, wobei ein mit Sauerstoff angereichertes Fluid von einer Kolonne der Vorrichtung zu einem Vergaser geleitet wird oder mindestens ein Teil der Luft, die für die Destillationsvorrichtung vorgesehen ist, von einem Kompressor (53) der Gasturbine stammt.
  12. Vorrichtung zur Produktion von Sauerstoff durch Tieftemperaturdestillation, umfassend:
    a) eine Hilfskolonne (25) und mindestens zwei andere Kolonnen (9, 18);
    b) Mittel, um einen Strom (1), der Sauerstoff, Stickstoff und Argon enthält, zu einer der anderen Kolonnen zu leiten;
    c) Mittel, um einen mit Sauerstoff angereicherten Strom (37) aus einer der anderen Kolonnen abzuziehen;
    d) Mittel, um einen Strom (29), der mindestens Argon und Sauerstoff enthält, aus einer der anderen Kolonnen abzuziehen, und Mittel, um diesen Strom als Versorgung zu der Hilfskolonne (25) zu leiten;
    e) Mittel, um ein mit Argon angereichertes Fluid aus der Hilfskolonne abzuziehen; und
    f) eine Entspannungsturbine (55);
    dadurch gekennzeichnet, dass die Hilfskolonne zwischen 1 und 99 theoretische Böden umfasst und Mittel vorhanden sind, um ein Gas (54) von der Kolonne, die mit dem niedrigsten Druck (18) arbeitet, abgesehen von der Hilfskolonne, zu der Entspannungsturbine zu leiten, wobei diese Mittel keine Verdichtungsmittel umfassen, und Mittel vorgesehen sind, um mindestens einen Teil des mit Argon angereicherten Stroms zu einer Entspannungsmaschine einer Gasturbine (51) zu leiten.
  13. Vorrichtung nach Anspruch 12, wobei zwischen der Kolonne (18), welche die Hilfskolonne versorgt, und der Hilfskolonne (25) kein Druckmindermittel vorgesehen ist.
  14. Vorrichtung nach Anspruch 12, umfassend Mittel, um mindestens einen Teil des mit Argon angereicherten Fluids an die Atmosphäre zu leiten, und/oder Mittel, um mindestens einen Teil des mit Argon angereicherten Fluids zu Adsorptionsmittelschüttungen oder umschaltbaren Wärmetauschern zu leiten, um sie zu regenerieren, und/oder Mittel, um mindestens einen Teil des mit Argon angereicherten Fluids mit einem mit Stickstoff angereicherten Gas (47) der Vorrichtung oder einer anderen Vorrichtung zu vermischen.
EP01400749A 2000-04-04 2001-03-22 Verfahren und Vorrichtung zur Erzeugung von sauerstoffreicher Flüssigkeit durch kryogenische Luftzerlegung Expired - Lifetime EP1143216B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0004284A FR2807150B1 (fr) 2000-04-04 2000-04-04 Procede et appareil de production d'un fluide enrichi en oxygene par distillation cryogenique
FR0004284 2000-04-04

Publications (2)

Publication Number Publication Date
EP1143216A1 EP1143216A1 (de) 2001-10-10
EP1143216B1 true EP1143216B1 (de) 2012-03-07

Family

ID=8848848

Family Applications (1)

Application Number Title Priority Date Filing Date
EP01400749A Expired - Lifetime EP1143216B1 (de) 2000-04-04 2001-03-22 Verfahren und Vorrichtung zur Erzeugung von sauerstoffreicher Flüssigkeit durch kryogenische Luftzerlegung

Country Status (6)

Country Link
US (1) US6434973B2 (de)
EP (1) EP1143216B1 (de)
JP (1) JP2001349669A (de)
AT (1) ATE548619T1 (de)
ES (1) ES2382453T3 (de)
FR (1) FR2807150B1 (de)

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2823256B1 (fr) * 2001-04-10 2003-07-25 Air Liquide Procede d'alimentation en azote impur de la chambre de combusti0n d'une turbine a gaz combinee a une unite de distillation d'air, et installation de production d'energie electrique correspondante
US6546748B1 (en) * 2002-06-11 2003-04-15 Praxair Technology, Inc. Cryogenic rectification system for producing ultra high purity clean dry air
FR2874249A1 (fr) * 2004-08-10 2006-02-17 Air Liquide Procede et installation de separation d'air par distillation cryogenique
US20070095100A1 (en) * 2005-11-03 2007-05-03 Rankin Peter J Cryogenic air separation process with excess turbine refrigeration
FR2913758B3 (fr) * 2007-03-12 2009-11-13 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
FR2930629B1 (fr) * 2008-04-23 2010-05-07 Air Liquide Appareil et procede de separation d'air par distillation cryogenique
US20110138856A1 (en) * 2009-12-10 2011-06-16 Henry Edward Howard Separation method and apparatus
EP2634517B1 (de) * 2012-02-29 2018-04-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Vorrichtung zur Trennung von Luft durch kryogenische Destillation
EP2713128A1 (de) * 2012-10-01 2014-04-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Verfahren zur Abscheidung von Luft durch kryogene Destillation
WO2016146246A1 (de) * 2015-03-13 2016-09-22 Linde Aktiengesellschaft Anlage zur erzeugung von sauerstoff durch tieftemperaturzerlegung von luft
FR3074274B1 (fr) * 2017-11-29 2020-01-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d'air par distillation cryogenique
US12352496B2 (en) * 2022-07-28 2025-07-08 Praxair Technology, Inc. Air separation unit and method for cryogenic separation of air using a distillation column system including an intermediate pressure kettle column
EP4592627A1 (de) * 2024-01-26 2025-07-30 Linde GmbH Verfahren zur kryogenen luftzerlegung und luftzerlegungsanlage

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0540900A1 (de) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Kryogenisches Rektifikationssystem zur Herstellung von ultrahochreinem Sauerstoff
EP0952415A1 (de) * 1998-04-21 1999-10-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Rektifikationsverfahren und -vorrichtung zur variablen Argon Herstellung

Family Cites Families (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3336427A1 (de) * 1983-10-06 1985-04-18 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zum regenerieren von adsorbern
JPS6428478A (en) * 1987-07-23 1989-01-31 Kobe Steel Ltd Path switching of switching type main heat exchanger for air separator
JP2789113B2 (ja) * 1989-07-07 1998-08-20 日本酸素株式会社 アルゴンの回収方法
FR2650378A1 (fr) * 1989-07-28 1991-02-01 Air Liquide Installation de distillation d'air produisant de l'argon
ES2045960T5 (es) * 1990-01-23 1997-05-01 Praxair Technology Inc Sistema para la separacion criogenica de aire con una columna hibrida de argon.
FR2675567A1 (fr) * 1991-04-16 1992-10-23 Air Liquide Procede et installation de production d'argon.
US5159816A (en) * 1991-05-14 1992-11-03 Air Products And Chemicals, Inc. Method of purifying argon through cryogenic adsorption
US5133790A (en) * 1991-06-24 1992-07-28 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification method for producing refined argon
US5197296A (en) * 1992-01-21 1993-03-30 Praxair Technology, Inc. Cryogenic rectification system for producing elevated pressure product
US5245831A (en) * 1992-02-13 1993-09-21 Air Products And Chemicals, Inc. Single heat pump cycle for increased argon recovery
US5228296A (en) * 1992-02-27 1993-07-20 Praxair Technology, Inc. Cryogenic rectification system with argon heat pump
US5245832A (en) * 1992-04-20 1993-09-21 Praxair Technology, Inc. Triple column cryogenic rectification system
US5341646A (en) * 1993-07-15 1994-08-30 Air Products And Chemicals, Inc. Triple column distillation system for oxygen and pressurized nitrogen production
GB9412182D0 (en) * 1994-06-17 1994-08-10 Boc Group Plc Air separation
FR2728663B1 (fr) * 1994-12-23 1997-01-24 Air Liquide Procede de separation d'un melange gazeux par distillation cryogenique
GB9505645D0 (en) * 1995-03-21 1995-05-10 Boc Group Plc Air separation
US5590543A (en) * 1995-08-29 1997-01-07 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
EP0793069A1 (de) * 1996-03-01 1997-09-03 Air Products And Chemicals, Inc. Mit einem Aufkochkompressor versehener Generator für Sauerstoff von zwei Reinheitsgraden
US5722259A (en) * 1996-03-13 1998-03-03 Air Products And Chemicals, Inc. Combustion turbine and elevated pressure air separation system with argon recovery
GB9607200D0 (en) * 1996-04-04 1996-06-12 Boc Group Plc Air separation
JPH1082582A (ja) * 1996-09-06 1998-03-31 Nippon Sanso Kk 空気液化分離装置及びその起動方法
GB9623519D0 (en) * 1996-11-11 1997-01-08 Boc Group Plc Air separation

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0540900A1 (de) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Kryogenisches Rektifikationssystem zur Herstellung von ultrahochreinem Sauerstoff
EP0952415A1 (de) * 1998-04-21 1999-10-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Rektifikationsverfahren und -vorrichtung zur variablen Argon Herstellung

Also Published As

Publication number Publication date
FR2807150A1 (fr) 2001-10-05
US6434973B2 (en) 2002-08-20
ATE548619T1 (de) 2012-03-15
JP2001349669A (ja) 2001-12-21
FR2807150B1 (fr) 2002-10-18
US20010052243A1 (en) 2001-12-20
ES2382453T3 (es) 2012-06-08
EP1143216A1 (de) 2001-10-10

Similar Documents

Publication Publication Date Title
EP2122282B1 (de) Verfahren und vorrichtung zur trennung einer mischung aus kohlenmonoxid, methan, wasserstoff und stickstoff durch kryogene destillation
EP1143216B1 (de) Verfahren und Vorrichtung zur Erzeugung von sauerstoffreicher Flüssigkeit durch kryogenische Luftzerlegung
EP0547946A1 (de) Verfahren und Apparat zur Herstellung unreinen Sauerstoffs
EP1623172A1 (de) Verfahren und system zur herstellung von druckluftgas durch kryogene destillation von luft
EP1189003B1 (de) Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation
US5079923A (en) Process and apparatus for distillation of air to produce argon
FR3150578A3 (fr) Procédé et appareil de séparation d’air par distillation cryogénique
WO1999054673A1 (fr) Procede et installation de distillation d'air avec production d'argon
FR2831249A1 (fr) Procede et installation de separation d'air par distillation cryogenique
FR2819046A1 (fr) Procede et appareil de separation d'air par distillation cryogenique
FR2724011A1 (fr) Procede et installation de production d'oxygene par distillation cryogenique
EP1063485B1 (de) Vorrichtung und Verfahren zur Luftzerlegung durch Tieftemperaturrektifikation
FR2830928A1 (fr) Procede de separation d'air par distillation cryogenique et une installation pour la mise en oeuvre de ce procede
FR2837564A1 (fr) Procede et installation de production d'oxygene et/ou d'azote sous pression et d'argon pur
FR2787559A1 (fr) Procede et installation de separation d'air par distillation cryogenique
EP1132700B1 (de) Verfahren und Vorrichtung zur kryogenischen Luftzerlegung
FR2862004A1 (fr) Procede et installation d'enrichissement d'un flux gazeux en l'un de ses constituants
FR2782787A1 (fr) Procede et installation de production d'oxygene impur par distillation d'air
FR2777641A1 (fr) Procede et installation de distillation d'air avec production d'argon
FR2861841A1 (fr) Procede et appareil de separation d'air par distillation cryogenique
EP3913310A1 (de) Verfahren und gerät zur trennung von luft durch kryogene destillation
FR3135134A1 (fr) Procédé d’augmentation de la capacité d’un appareil de séparation d’air par distillation cryogénique existant et appareil de séparation d’air
FR2825453A1 (fr) Procede et installation de separation par distillation
FR2854232A1 (fr) Procede de distillation d'air pour produire de l'argon
FR2825454A3 (fr) Procede et appareil de separation d'air par distillation cryogenique

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE TR

AX Request for extension of the european patent

Free format text: AL;LT;LV;MK;RO;SI

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: L'AIR LIQUIDE, S.A. A DIRECTOIRE ET CONSEIL DE SUR

17P Request for examination filed

Effective date: 20020410

AKX Designation fees paid

Free format text: AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE TR

17Q First examination report despatched

Effective date: 20050110

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'E

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'E

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 548619

Country of ref document: AT

Kind code of ref document: T

Effective date: 20120315

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: FRENCH

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 60146212

Country of ref document: DE

Effective date: 20120503

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2382453

Country of ref document: ES

Kind code of ref document: T3

Effective date: 20120608

REG Reference to a national code

Ref country code: NL

Ref legal event code: T3

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120307

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120608

REG Reference to a national code

Ref country code: AT

Ref legal event code: MK05

Ref document number: 548619

Country of ref document: AT

Kind code of ref document: T

Effective date: 20120307

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120307

BERE Be: lapsed

Owner name: L'AIR LIQUIDE, S.A. POUR L'ETUDE ET L'EXPLOITATIO

Effective date: 20120331

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120307

Ref country code: MC

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20120331

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120709

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20120331

Ref country code: AT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120307

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20120331

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20120331

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120307

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20120322

26N No opposition filed

Effective date: 20121210

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 60146212

Country of ref document: DE

Effective date: 20121210

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20130326

Year of fee payment: 13

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20130320

Year of fee payment: 13

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20130327

Year of fee payment: 13

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20120307

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20120322

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20140319

Year of fee payment: 14

REG Reference to a national code

Ref country code: NL

Ref legal event code: V1

Effective date: 20141001

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20141001

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20140322

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20150428

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20140323

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20150322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20150322

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 16

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20160321

Year of fee payment: 16

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20160330

Year of fee payment: 16

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 60146212

Country of ref document: DE

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20171130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20171003

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20170331