EP1074805B1 - Procédé et dispositif pour la production d'oxygène sous pression - Google Patents

Procédé et dispositif pour la production d'oxygène sous pression Download PDF

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Publication number
EP1074805B1
EP1074805B1 EP99118724A EP99118724A EP1074805B1 EP 1074805 B1 EP1074805 B1 EP 1074805B1 EP 99118724 A EP99118724 A EP 99118724A EP 99118724 A EP99118724 A EP 99118724A EP 1074805 B1 EP1074805 B1 EP 1074805B1
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EP
European Patent Office
Prior art keywords
pressure
air
pressure column
low
column
Prior art date
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Revoked
Application number
EP99118724A
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German (de)
English (en)
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EP1074805A1 (fr
Inventor
Wilhelm Rohde
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Linde GmbH
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Linde GmbH
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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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • the invention relates to a method for the production of oxygen according to the Preamble of claim 1.
  • the invention is based on the object, such a method energetically cheaper.
  • the first pressure, on which the first and the second partial flow of the air in common be compacted, is slightly above the operating pressure of the pressure column.
  • the Pressure difference is preferably such that the first partial flow of the air Flow resistance between the air compressor and the pressure column without can overcome pressure-changing measures, and is for example 0.1 to 0.5 bar.
  • the operating pressures at the top of the rectification columns are for example 2.5 to 10 bar, preferably 4 to 7 bar in the pressure column and 1.05 to 4 bar, preferably 1.1 to 1.5 bar in the low pressure column.
  • an air compressor is the only one external used driven machine. This brings the total air to the first pressure, at the same time the inlet pressure of expansion machine and cold compressor represents.
  • the oxygen product can under a discharge pressure be obtained, for example, 0.5 to 4 bar, preferably 1 to 3 bar over the operating pressure of the low pressure column, without that an additional Energy consumption compared to the recovery of the oxygen product Low pressure column pressure is connected.
  • the cold-compressed partial air flow is in the indirect heat exchange with the evaporating oxygen at least partially, preferably completely or in the essentially completely condensed.
  • the condensate is then released and fed to the pressure column and / or the low pressure column.
  • the process of the invention is particularly for the production of impure Oxygen with a purity of 80 to 99.5 mol%, preferably 90 to 95 mol% suitable under superatmospheric pressure.
  • the process stream, the work performing relaxation is subjected, however, by a third partial flow of the first pressure formed compressed compressed air.
  • the indirect heat exchange in which the Product oxygen vaporizes against the condensing second partial stream of air, in the main heat exchanger.
  • the Separate secondary condenser provided as the main heat exchanger Circulation evaporator is formed;
  • a Countercurrent heat exchanger or a falling film evaporator as secondary condenser use.
  • the Brake device can, for example, by a brake fan and / or a Brake generator can be formed and located outside the coldbox, the to Insulation of the cold parts of the apparatus is used. This can give energy to the Given environment and thus won the necessary for the process cold be without an additional relaxation machine is used.
  • relaxation machine, cold compressor and braking device immediately mechanically coupled, for example via a common shaft.
  • the invention also relates to a device according to claim 5.
  • Atmospheric air 1 is after flowing through a filter 2 in an air compressor 3 compressed to a first pressure, which is approximately equal to the operating pressure of the pressure column 13 is. (To overcome the line losses, the first pressure must be slightly above the Pressure column pressure are, for example, less than 1 bar, preferably 0.5 bar or less.)
  • After removal of the compression heat in the aftercooler 4 flows compressed air to the first pressure 5 to a cleaning device 6, by a A pair of reversible molecular electroluminescent adsorbents is formed.
  • the first Pressure compressed air flows after cleaning 6 via line 7 to Main heat exchanger 8 and is cooled there in part to about dew point.
  • the cold air 9 is at 10 in a first partial flow 11 and a second partial flow 12th divided up.
  • the first partial flow 11 is directly into the pressure column 13 of the Rectifier fed directly above the sump.
  • the Rectification system also has a low-pressure column 14, which has a common condenser-evaporator, the main capacitor 15 in Heat exchange relationship with the pressure column 13 is.
  • the second partial flow 12 is in a cold compressor 16 to a second, higher Pressure, via line 17 to a secondary capacitor 18, as Circulation evaporator is madebiildet (not shown), guided, and there essential completely liquefied.
  • the liquefied air 19 is via a valve 20 in the pressure column 13 throttled, either at the bottom (see drawing) or at an intermediate point, some theoretical or practical soils above the feed of the first partial flow 11 is located.
  • Another proportion of the first pressure compressed and then purified Air 7 is at an intermediate temperature from the main heat exchanger. 8 led out and forms the third partial flow 21.
  • This is in a Relaxation turbine 22 work-performing relaxed to about low-pressure column pressure and passed via line 23 directly to the low pressure column 14.
  • the relaxation turbine 22 is over a common shaft with the cold compressor 16 and not one coupled brake generator coupled.
  • Liquid raw oxygen 24 from the bottom of the pressure column 13 and liquid nitrogen 25 from the main condenser 15 are cooled in the subcooling countercurrent 26 and abandoned via the valves 27 and 28 to the low-pressure column 14.
  • nitrogen-rich residual gas 29 is withdrawn and after heating in the subcooling countercurrent 26 and in the main heat exchanger. 8 discharged via line 30. It can also be used as a regeneration gas in the Cleaning device 6 are used (not shown).
  • liquid oxygen falls with the required purity.
  • a part is withdrawn via line 31 liquid, by means a pump 32 brought to the required discharge pressure and under this pressure evaporated in the secondary condenser 18.
  • the gaseous pressure oxygen product flows via line 33 to the main heat exchanger and is via line 34 below about Ambient temperature delivered.

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

Claims (8)

  1. Procédé pour la production d'oxygène sous pression par séparation de l'air à basse température dans un système de rectification, qui présente au moins une colonne de pression (13) et une colonne de basse pression (14), dans lequel l'air utilisé (1) est compressé (3) à une première pression, qui est approximativement similaire à la pression de fonctionnement de la colonne de pression (13), au moins un premier courant partiel (11) de l'air utilisé (1) est refroidi par la première pression dans un échangeur de chaleur principal (8) et est introduit dans la colonne de pression (13), dans lequel un deuxième courant partiel (12,17) de l'air utilisé (1) compressé à la première pression est amené à une deuxième pression (16), dans lequel un courant d'oxygène (31) est extrait de la colonne de basse pression (14), amené (32) à l'état liquide à une pression d'émission, qui est supérieure à la pression de fonctionnement de la colonne de basse pression (14), évaporé par échange de chaleur indirect (18) avec le deuxième courant partiel (12,17) en aval de la compression (16) à la deuxième pression, réchauffé dans l'échangeur de chaleur principal (8) et délivré comme produit (34) et dans lequel le fluide de travail d'un courant de processus (21) subit une expansion (22) et est introduit (23) dans la colonne de basse pression (14), caractérisé en ce que le deuxième courant partiel (12) est amené à la deuxième pression en amont de l'échange de chaleur indirect (18) au moyen d'un compresseur froid (16) et en ce que au moins une partie de l'énergie mécanique produite lors de l'expansion (22) du fluide de travail est utilisée pour entraíner le compresseur froid (16).
  2. Procédé selon la revendication 1, caractérisé en ce que le courant de processus, qui est subordonné à l'expansion (22) du fluide de travail, est formé par un troisième courant partiel (21) de l'air utilisé (1) compressé à la première pression.
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que l'échange de chaleur indirect est effectué dans un compresseur annexe (18) séparé de l'échangeur de chaleur principal (8).
  4. Procédé selon une des revendications 1 à 3, caractérisé en ce que une partie de l'énergie mécanique produite pendant l'expansion (22) du fluide de travail est délivrée à un dispositif de freinage.
  5. Dispositif pour la production d'oxygène sous pression par séparation de l'air à basse température, comportant un système de rectification, qui présente au moins une colonne de pression (13) et une colonne de basse pression (14), comportant un compresseur d'air (3) pour compresser l'air utilisé (1) à une première pression, qui est approximativement similaire à la pression de fonctionnement de la colonne de pression (13), comportant une première conduite d'air partiel (5,7,9,11), qui est reliée au compresseur d'air (3) et à la colonne de pression (13) et passe à travers un échangeur de chaleur principal (8), comportant une conduite de production d'oxygène (31,33,34), qui est reliée à la colonne de basse pression (14), présente un moyen (32) d'augmentation de la pression, est réalisée entre la colonne de basse pression (14) et le moyen (32) d'augmentation de la pression comme une conduite de liquides et est reliée à l'espace d'évaporation d'un compresseur-évaporateur (18), comportant une deuxième conduite d'air partiel (5,7,9,12,17), qui mène du compresseur d'air (3) à l'espace de liquéfaction du compresseur-évaporateur (18) en passant par un surpresseur (16) et comportant une machine d'expansion (22), caractérisé en ce que le surpresseur est réalisé comme un compresseur froid (16) et en ce que la machine d'expansion (22) est couplée au compresseur froid (16).
  6. Dispositif selon la revendication 5, caractérisé par une troisième conduite d'air partiel (21), qui mène du compresseur d'air (3) à la machine d'expansion (22).
  7. Dispositif selon la revendication 5 ou 6, caractérisé en ce que le compresseur-évaporateur (18) est formé par un compresseur annexe (18) séparé de l'échangeur de chaleur principal (8).
  8. Dispositif selon une des revendications 5 à 7, caractérisé en ce que la machine d'expansion (22) est couplée à un dispositif de freinage.
EP99118724A 1999-08-05 1999-09-22 Procédé et dispositif pour la production d'oxygène sous pression Revoked EP1074805B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19936816 1999-08-05
DE19936816A DE19936816A1 (de) 1999-08-05 1999-08-05 Verfahren und Vorrichtung zur Gewinnung von Sauerstoff unter überatmosphärischem Druck

Publications (2)

Publication Number Publication Date
EP1074805A1 EP1074805A1 (fr) 2001-02-07
EP1074805B1 true EP1074805B1 (fr) 2005-01-19

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ID=7917229

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99118724A Revoked EP1074805B1 (fr) 1999-08-05 1999-09-22 Procédé et dispositif pour la production d'oxygène sous pression

Country Status (5)

Country Link
US (1) US6332337B1 (fr)
EP (1) EP1074805B1 (fr)
AT (1) ATE287518T1 (fr)
DE (2) DE19936816A1 (fr)
ES (1) ES2237008T3 (fr)

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DE102007031765A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
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EP2312248A1 (fr) 2009-10-07 2011-04-20 Linde Aktiengesellschaft Procédé et dispositif de production d'oxygène sous pression et de crypton/xénon
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2520886A1 (fr) 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
DE102011112909A1 (de) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
EP2600090B1 (fr) 2011-12-01 2014-07-16 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
EP2784420A1 (fr) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
EP2801777A1 (fr) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
EP2963371B1 (fr) 2014-07-05 2018-05-02 Linde Aktiengesellschaft Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2963369B1 (fr) 2014-07-05 2018-05-02 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
PL2963370T3 (pl) 2014-07-05 2018-11-30 Linde Aktiengesellschaft Sposób i urządzenie do kriogenicznego rozdziału powietrza

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FR2724011B1 (fr) * 1994-08-29 1996-12-20 Air Liquide Procede et installation de production d'oxygene par distillation cryogenique
US5765396A (en) * 1997-03-19 1998-06-16 Praxair Technology, Inc. Cryogenic rectification system for producing high pressure nitrogen and high pressure oxygen

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EP1074805A1 (fr) 2001-02-07
DE19936816A1 (de) 2001-02-08
ES2237008T3 (es) 2005-07-16
ATE287518T1 (de) 2005-02-15
DE59911495D1 (de) 2005-02-24
US6332337B1 (en) 2001-12-25

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