EP1143216A1 - Verfahren und Vorrichtung zur Erzeugung von sauerstofreicher Flüssigkeit durch kryogenische Luftzerlegung - Google Patents

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

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Publication number
EP1143216A1
EP1143216A1 EP01400749A EP01400749A EP1143216A1 EP 1143216 A1 EP1143216 A1 EP 1143216A1 EP 01400749 A EP01400749 A EP 01400749A EP 01400749 A EP01400749 A EP 01400749A EP 1143216 A1 EP1143216 A1 EP 1143216A1
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European Patent Office
Prior art keywords
argon
enriched
flow
column
oxygen
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EP01400749A
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English (en)
French (fr)
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EP1143216B1 (de
Inventor
Benoít Davidian
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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
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP1143216A1 publication Critical patent/EP1143216A1/de
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—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
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—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
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    • F25J2200/00—Processes or apparatus using separation by rectification
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    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
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    • 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
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    • 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
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
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    • 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 production method and apparatus of a fluid enriched in oxygen by cryogenic distillation of a mixture containing nitrogen, oxygen and argon.
  • it relates to a method and an apparatus for separating air by cryogenic distillation allowing the production of pure oxygen, i.e. oxygen containing at least 95% mol. oxygen, preferably at least 98% mol. oxygen or even 99.5% mol. oxygen.
  • Patent application EP-A-0540900 describes a production process impure oxygen in which part of the impure argon containing at least 90% of argon from a column of mixture is mixed with the residual nitrogen from a simple column.
  • the mixing column operates at the same low pressure as the low column pressure, 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-A-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 describes a process for the production of 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 pressure substantially identical above 2.5 bara. No argon gas flow is produced.
  • EP-A-0952415 describes an apparatus comprising a double column and a argon column operating with a yield lower than the optimal yield.
  • An object of the present invention is to increase the yield of pure oxygen an air separation device.
  • Another object of the invention is to provide an air separation device particularly well suited to the demands of large quantities of nitrogen under pressure (typically when integrated with an IGCC gas turbine).
  • the flow enriched in argon or the flow enriched in argon mixed with a gas enriched in nitrogen can be sent upstream of the expansion machine of a gas turbine.
  • the flow enriched in argon can contain between 10 and 95 mol%. argon (or between 40 and 95% mol. argon), between 2 and 40.% mol of oxygen and between 2 and 40% mol. nitrogen.
  • the flow enriched in argon which is released to the atmosphere and / or which is used to regenerate adsorbent beds or reversible exchangers and / or which is mixed with a gas enriched in nitrogen from the device and / or another device and / or which 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 best to mix the flow enriched in argon with a gas enriched in nitrogen containing at least 90% mol.
  • 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 include an auxiliary separation column a flow containing at least argon and oxygen and two other columns, of which a high pressure column and a low pressure column thermally connected between them, the auxiliary column being supplied from the low pressure column.
  • the apparatus may include an auxiliary separation column of a flow rate containing at least argon and oxygen and at least three others columns, including a high pressure column, an intermediate pressure column and a low pressure column thermally connected to each other, the auxiliary column being supplied from the low pressure column or the intermediate pressure column.
  • an integrated method of separation comprising a method according to one of claims 1 to 12 in which a nitrogen-enriched gas is sent from the operating column preferably at the lowest pressure at the gas turbine, after one step possible compression and, optionally, a fluid enriched with oxygen is sent from an appliance column to a gasifier.
  • the auxiliary column contains between 30 and 40 trays theoretical.
  • the separation of oxygen and argon in the low pressure column tank is facilitated.
  • the fluid enriched in argon withdrawn from the auxiliary column is not necessarily an end product of the device but can be used to cool flows re-entering the columns or supplying frigories by expansion.
  • Figure 1 is a diagram of an oxygen production apparatus according to the invention using a double column.
  • Figure 2 is a diagram of an oxygen production apparatus according to the invention using a triple column.
  • an air flow 1 of 1000Nm3 / h is purified by beds adsorbent 4 is divided into two.
  • the flow 2 is boosted at a higher pressure, sent to the heat exchanger 3 where it cools ensuring the vaporization of liquid oxygen and then to a hydraulic turbine 5 where it comes out at least partially liquid.
  • This liquid (or two-phase mixture) 7 is sent to the column high pressure 9 operating between 14 and 15 bar and possibly partly at the column low pressure 11 operating between 4 and 6 bar (or even between 2 and 10 bar), either sending part of the capacity liquid upstream of the medium pressure column either by withdrawing a flow having a composition similar to that of the liquid air of the high pressure column 9, as shown in Figure 1.
  • the device may include an insufflation turbine which serves during start-up or a low-pressure nitrogen turbine 55.
  • a flow of rich liquid 15 is withdrawn from the high pressure column and sent to the sub-cooler 17, divided in two and sent in part to the lower column pressure, after expansion in the valve 21 and in part at the head condenser 23 of the auxiliary column 25 after expansion in the valve 27. At least the rich liquid partially vaporized in the overhead condenser is sent to the lower column pressure 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 19 can optionally be withdrawn from the head of the high pressure column 9.
  • the auxiliary column is supplied by a gas flow 29 containing between 5 and 15% mol. argon, preferably around 7 mol%. argon.
  • the tank 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 can alternatively be supplied with a liquid flow containing between 5 and 15 mol%. argon, preferably around 7 mol%. argon.
  • column 25 will have a tank reboiler, heated by a gas flow such as air or nitrogen from the high pressure column 9.
  • a liquid air flow 33 and a lean liquid flow 35 are sent from the high pressure column 9 to low pressure column 11, after having been sub-cooled in the sub-cooler 17 and expanded in valves.
  • a liquid oxygen flow 37 containing 99.5% mol. oxygen is drawn in low pressure column tank, pressurized by a pump 39 and vaporized in the exchanger 3.
  • the mixture 53 heats up in the sub-cooler 17 then heats up in the exchanger 3.
  • the mixture can then be discharged into the atmosphere and / or can be used to regenerate the adsorbent beds 4 or reversible exchangers and / or sent in upstream of the expansion machine 51 of a gas turbine after a step of compression.
  • part of the mixture 53 can be expanded in a turbine 55 (dotted line).
  • a triple column is used in place of the double column of Figure 1.
  • An air flow 1 is purified by adsorbent beds 4 is divided into two.
  • Flow 2 is boosted to a higher pressure, sent to the heat exchanger heat 3 where it cools by ensuring the vaporization of liquid oxygen and then at a hydraulic turbine 5 where it exits 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 at the low pressure column 11 operating between 4 and 6 bar and / or possibly at the intermediate pressure column 40 operating between 7 and 9 bar, either by sending part of the liquid of a capacity upstream of the middle column pressure either by withdrawing a flow having a composition similar to that of liquid air of the high pressure column 9, as shown in FIG. 2.
  • the device may include an insufflation turbine which serves during start-up or a low-pressure nitrogen turbine 55.
  • a flow of rich liquid 15 is withdrawn from the high pressure column and sent to the sub-cooler 17, divided in two and sent partly to the middle of the column operating at intermediate pressure 40, after expansion in valve 21 and partly at head condenser 23 of the auxiliary column 25 after expansion in the valve 27.
  • the at least partially vaporized rich liquid in the overhead condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a flow gases are sent from the condenser to the low pressure column.
  • a nitrogen gas flow 19 can optionally be withdrawn from the head of the high pressure column 9.
  • the auxiliary column is supplied with part of a gas flow 29 containing between 5 and 15 mol%. argon, preferably around 7 mol%. argon.
  • the liquid tank 31 of the auxiliary column is returned to the low pressure column which operates at substantially the same pressure as the auxiliary column.
  • the auxiliary column 25 can alternatively be supplied with a liquid flow containing between 5 and 15 mol%. argon, preferably around 7 mol%. argon.
  • column 25 will have a tank reboiler, heated by a gas flow such as air or nitrogen from the high pressure column 9.
  • the rest of the gas flow 29 is used to heat the tank reboiler 41 of the column 40 and after condensation is returned to the low pressure column with the flow rate 31.
  • the tank liquid 43 of the column 40 is partly sent directly to the low pressure column and partly to the condenser at the top of column 40 where it at least partially vaporizes before being sent to the low pressure column at its tower.
  • the overhead liquid 47 of the column 40 is sub-cooled in the exchanger 17, expanded, mixed with expanded flow 35 and sent to the top of the lower column pressure.
  • a liquid air flow 33 and a lean liquid flow 35 are sent from the high pressure column 9 to low pressure column 11, after having been sub-cooled in the sub-cooler 17 and expanded in valves.
  • a liquid oxygen flow 37 containing 99.5% mol. oxygen is drawn in low pressure column tank, pressurized by a pump 39 and vaporized in the exchanger 3.
  • the mixture 53 heats up in the sub-cooler 17 then heats up in the exchanger 3.
  • the mixture can then be discharged into the atmosphere and / or can be used to regenerate the adsorbent beds 4 or reversible exchangers and / or sent in upstream of the expansion machine 51 of a gas turbine after a step of possible compression.
  • part of the mixture 53 can be expanded in a turbine 55 (dotted line).
  • the method according to the invention is of particular interest in the case in which the nitrogen in the low pressure column is valued, for example by sending it to an expansion machine 51 of a gas turbine.
  • at least part of the air 1 can come from compressor 53 of the gas turbine and the oxygen produced by the device distillation can be used for the gasification necessary to produce the fuel for the gas turbine.

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

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

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EP1143216B1 EP1143216B1 (de) 2012-03-07

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AT (1) ATE548619T1 (de)
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FR (1) FR2807150B1 (de)

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WO2016146246A1 (de) * 2015-03-13 2016-09-22 Linde Aktiengesellschaft Anlage zur erzeugung von sauerstoff durch tieftemperaturzerlegung von luft

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FR2874249A1 (fr) * 2004-08-10 2006-02-17 Air Liquide Procede et installation de separation d'air par distillation cryogenique
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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
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
FR3137747B1 (fr) * 2022-07-05 2024-07-12 Air Liquide Procédé de régulation d’un appareil de séparation d’air par distillation cryogénique
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
CN117367034A (zh) * 2023-11-01 2024-01-09 河北荣信钢铁有限公司 一种快速检修供氧的空分制氧方法及装置
EP4592627A1 (de) * 2024-01-26 2025-07-30 Linde GmbH Verfahren zur kryogenen luftzerlegung und luftzerlegungsanlage

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WO2016146246A1 (de) * 2015-03-13 2016-09-22 Linde Aktiengesellschaft Anlage zur erzeugung von sauerstoff durch tieftemperaturzerlegung von luft
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US20010052243A1 (en) 2001-12-20
ATE548619T1 (de) 2012-03-15
EP1143216B1 (de) 2012-03-07
US6434973B2 (en) 2002-08-20
ES2382453T3 (es) 2012-06-08
FR2807150A1 (fr) 2001-10-05
FR2807150B1 (fr) 2002-10-18
JP2001349669A (ja) 2001-12-21

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