EP0612967B1 - Verfahren zur Herstellung von Sauerstoff und/oder Stickstoff unter Druck - Google Patents

Verfahren zur Herstellung von Sauerstoff und/oder Stickstoff unter Druck Download PDF

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Publication number
EP0612967B1
EP0612967B1 EP94400372A EP94400372A EP0612967B1 EP 0612967 B1 EP0612967 B1 EP 0612967B1 EP 94400372 A EP94400372 A EP 94400372A EP 94400372 A EP94400372 A EP 94400372A EP 0612967 B1 EP0612967 B1 EP 0612967B1
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EP
European Patent Office
Prior art keywords
pressure
air
column
turbine
liquid
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
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EP94400372A
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English (en)
French (fr)
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EP0612967A1 (de
Inventor
Norbert Rieth
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Air Liquide SA
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
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
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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
    • F25J3/04248—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
    • F25J3/04006—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • EP-A-0.420.725 describes a liquefier which uses a Claude turbine and a second low pressure air turbine.
  • the invention aims to improve the energy performance of known methods.
  • the installation shown in Figure 1 is intended to produce gaseous oxygen at a high pressure of approximately 3 to 100 bars, nitrogen gas at a low pressure of approximately 1.7 to 5 bars, oxygen liquid and liquid nitrogen.
  • This installation essentially comprises: a main air compressor 1; a pre-cooler 2; an adsorption purification device 3; a blower-turbine assembly comprising a blower 4 and a turbine 5, the wheels of which are fixed on the same shaft; an atmospheric or water cooler 6 for the fan; a heat exchange line 7; a second expansion turbine 8 braked by an alternator 9; a double distillation column 10 comprising a medium-pressure column 11 and a low-pressure column 12 coupled by a vaporizer-condenser 13 which places the head nitrogen of column 11 in heat exchange relationship with the liquid oxygen from the bottom column 12; a liquid oxygen pump 14; storage of liquid oxygen at atmospheric pressure; a storage 16 of liquid nitrogen at atmospheric pressure; a separator pot 17; and a sub-cooler 18.
  • the column 12 is under a pressure of approximately 1.7 to 5 bars, and the column 11 under the corresponding pressure of approximately 6.5 to 16 bars.
  • All the air to be distilled is compressed in 1, pre-cooled in 2 to + 5 to + 10 ° C, purified in water and CO2 in 3 and boosted in 4 at high pressure. After pre-cooling in 6 then partial cooling in 7 to an intermediate temperature T1, part of the air under high pressure continues to cool in the heat exchange line, is liquefied and then divided into two fractions. Each fraction is expanded in a respective expansion valve 19, 20, then introduced into the respective column 11, 12.
  • “rich liquid” (oxygen-enriched air) drawn off from the bottom of column 11 and “lean liquid” (almost pure nitrogen) drawn off at the top of this column are, after sub-cooling in 18 and expansion in respective expansion valves 21 and 22, introduced at an intermediate level and at the head, respectively, of the column 12.
  • Liquid oxygen is withdrawn from the tank of column 12. A fraction goes directly, after sub-cooling in 18 and expansion to atmospheric pressure in an expansion valve 23, in storage 15, while the rest is brought by the pump 14 at the desired high production pressure, then vaporized and warmed to room temperature in the heat exchange line before being recovered via a line 24.
  • liquid nitrogen under medium pressure drawn off at the top of column 11, is sub-cooled at 18, expanded at atmospheric pressure in an expansion valve 25, and introduced into the separator pot 17.
  • the phase liquid is sent to storage 16, while the vapor phase is reheated in 18 and then in 7 and recovered as a product (nitrogen low pressure gas) via a line 26.
  • the waste gas (impure nitrogen WN2) withdrawn at the head of column 12 is preheated in 18 and then partially reheated in 7, to an intermediate temperature T2. At this temperature, the waste gas is removed from the heat exchange line, expanded to atmospheric pressure in the turbine 8, which cools it, and reintroduced into the heat exchange line at the corresponding temperature, to then be reheated at room temperature and discharged via line 27.
  • the heat exchange diagram of Figure 2 was obtained by calculation with a low pressure of 2.2 bars, a medium pressure of 8.2 bars, a high air pressure of 32 bars and a high oxygen pressure 40 bars.
  • the inlet temperature T1 of the turbine 5 is slightly lower than the oxygen vaporization stage P, and the inlet temperature T2 of the turbine 8 is close to the knee G of air liquefaction.
  • the point R of the warming curve corresponds to the reintroduction into the exchange line of the turbinated residual gas, and the section of curve with increased slope, between this point R and the temperature T2, brings a tightening of the diagram in the corresponding cold part. thermodynamic improvement of the process.
  • the operation under pressure of column 12 results in a reduction in the purity of the oxygen produced.
  • the high pressure oxygen gas and the liquid oxygen stored at 15 typically have a purity of the order of 95%.
  • the invention also applies to the production of nitrogen gas under high pressure, brought by a pump (not shown) to the desired high pressure and then vaporized in the heat exchange line, and / or to the production of oxygen. and / or nitrogen under several pressures, using several high air pressures.
  • the vaporization of the liquid or liquids can be carried out in a manner not concomitant with the liquefaction of air, as in the example described above, or concomitantly with this liquefaction.

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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)

Claims (5)

  1. Verfahren zur Herstellung von gasförmigem Sauerstoff und/oder gasförmigem Stickstoff unter Druck, bei dem:
    - Luft in einer Doppel-Destillationskolonne (10) destilliert wird, die eine Niederdruckkolonne (12), die unter einem Druck arbeitet, der Niederdruck genannt wird, und eine Mitteldruckkolonne (11), die unter einem Druck arbeitet, der Mitteldruck genannt wird, umfaßt;
    - die gesamte zu destillierende Luft auf zumindest einen hohen Druck, der deutlich höher ist als der Mitteldruck, verdichtet wird (bei 1, 4);
    - die verdichtete Luft auf eine Zwischentemperatur abgekühlt wird und ein Teil davon in einer Turbine (5) vor Einleiten in die Mitteldruckkolonne (11) auf den Mitteldruck entspannt wird;
    - die nicht durch die Turbine geleitete Luft verflüssigt wird, dann nach Entspannung (bei 19, 20) in die Doppelkolonne eingeleitet wird; und
    - zumindest ein aus der Doppelkolonne entnommenes flüssiges Produkt auf den Produktionsdruck gebracht wird und dieses flüssige Produkt durch Wärmeaustausch mit der Luft verdampft wird,
    dadurch gekennzeichnet, daß :
    - die Niederdruckkolonne (12) unter Druck betrieben wird; und
    - das restliche Gas aus dem Kopf der Niederdruckkolonne, nachdem es teilweise erwärmt wurde, in einer zweiten Turbine (8) entspannt wird, und daß die Eintrittstemperatur (T2) der zweiten Turbine (8) in der Nähe des Verflüssigungspunktes (G) oder des Hauptverflüssigungspunktes der Luft liegt.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Niederdruckkolonne (12) unter etwa 1,7 bis 5 bar betrieben wird und die Mitteldruckkolonne (11) unter einem entsprechenden Druck von etwa 6,5 bis 16 bar betrieben wird.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß die Eintrittstemperatur der Luftturbine (5) höher ist als die Eintrittstemperatur der zweiten Turbine (8).
  4. Verfahren nach einem der vorangehenden Ansprüche, bei dem flüssiger Sauerstoff, der zur Verdampfung durch Wärmeaustausch mit der Luft vorgesehen ist, einige Böden oberhalb einer Entnahme von flüssigem Sauerstoff, der für einen Lagerbehälter (15) vorgesehen ist, entnommen wird.
  5. Verfahren nach einem der Ansprüche 1 bis 3, bei dem das flüssige Produkt oder eines der flüssigen Produkte flüssiger Stickstoff ist.
EP94400372A 1993-02-25 1994-02-22 Verfahren zur Herstellung von Sauerstoff und/oder Stickstoff unter Druck Expired - Lifetime EP0612967B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9302137A FR2702040B1 (fr) 1993-02-25 1993-02-25 Procédé et installation de production d'oxygène et/ou d'azote sous pression.
FR9302137 1993-02-25

Publications (2)

Publication Number Publication Date
EP0612967A1 EP0612967A1 (de) 1994-08-31
EP0612967B1 true EP0612967B1 (de) 1997-04-23

Family

ID=9444399

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94400372A Expired - Lifetime EP0612967B1 (de) 1993-02-25 1994-02-22 Verfahren zur Herstellung von Sauerstoff und/oder Stickstoff unter Druck

Country Status (10)

Country Link
US (1) US5515688A (de)
EP (1) EP0612967B1 (de)
JP (1) JPH06249574A (de)
CN (1) CN1081780C (de)
AU (1) AU672859B2 (de)
CA (1) CA2116297C (de)
DE (1) DE69402745T2 (de)
ES (1) ES2102780T3 (de)
FR (1) FR2702040B1 (de)
ZA (1) ZA941279B (de)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5355682A (en) † 1993-09-15 1994-10-18 Air Products And Chemicals, Inc. Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen
FR2730172B1 (fr) * 1995-02-07 1997-03-21 Air Liquide Methode et appareil de surveillance de fonctionnement d'une installation de separation d'air
US5924307A (en) * 1997-05-19 1999-07-20 Praxair Technology, Inc. Turbine/motor (generator) driven booster compressor
US20070095100A1 (en) * 2005-11-03 2007-05-03 Rankin Peter J Cryogenic air separation process with excess turbine refrigeration
US7552599B2 (en) * 2006-04-05 2009-06-30 Air Products And Chemicals, Inc. Air separation process utilizing refrigeration extracted from LNG for production of liquid oxygen
US9714789B2 (en) * 2008-09-10 2017-07-25 Praxair Technology, Inc. Air separation refrigeration supply method
DE102011113262A1 (de) * 2011-09-13 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft
CN109737691B (zh) * 2019-01-31 2020-05-19 东北大学 一种钢铁企业空气分离系统

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1148546A (fr) * 1956-09-27 1957-12-11 Air Liquide Procédé de séparation de l'air en ses éléments
GB943669A (en) * 1961-11-03 1963-12-04 Petrocarbon Dev Ltd Separation of oxygen from air
DE1501722A1 (de) * 1966-01-13 1969-06-26 Linde Ag Verfahren zur Tieftemperatur-Luftzerlegung zur Erzeugung von hochverdichtetem gasfoermigem und/oder fluessigem Sauerstoff
US3375673A (en) * 1966-06-22 1968-04-02 Hydrocarbon Research Inc Air separation process employing work expansion of high and low pressure nitrogen
US3589137A (en) * 1967-10-12 1971-06-29 Mc Donnell Douglas Corp Method and apparatus for separating nitrogen and hydrocarbons by fractionation using the fluids-in-process for condenser and reboiler duty
DE2535132C3 (de) * 1975-08-06 1981-08-20 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zur Herstellung von Drucksauerstoff durch zweistufige Tieftemperaturrektifikation von Luft
BR7606681A (pt) * 1975-10-28 1977-11-16 Linde Ag Processo e instalacao para fracionamento de ar
FR2461906A1 (fr) * 1979-07-20 1981-02-06 Air Liquide Procede et installation cryogeniques de separation d'air avec production d'oxygene sous haute pression
GB2129115B (en) * 1982-10-27 1986-03-12 Air Prod & Chem Producing gaseous nitrogen
FR2652409A1 (fr) * 1989-09-25 1991-03-29 Air Liquide Procede de production frigorifique, cycle frigorifique correspondant et leur application a la distillation d'air.
GB9015377D0 (en) * 1990-07-12 1990-08-29 Boc Group Plc Air separation
JP2909678B2 (ja) * 1991-03-11 1999-06-23 レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 圧力下のガス状酸素の製造方法及び製造装置

Also Published As

Publication number Publication date
CN1093158A (zh) 1994-10-05
FR2702040A1 (fr) 1994-09-02
DE69402745T2 (de) 1997-11-13
ES2102780T3 (es) 1997-08-01
JPH06249574A (ja) 1994-09-06
CN1081780C (zh) 2002-03-27
ZA941279B (en) 1994-09-30
US5515688A (en) 1996-05-14
AU5634794A (en) 1994-09-01
DE69402745D1 (de) 1997-05-28
FR2702040B1 (fr) 1995-05-19
CA2116297C (fr) 2004-12-07
AU672859B2 (en) 1996-10-17
CA2116297A1 (fr) 1994-08-26
EP0612967A1 (de) 1994-08-31

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