EP0042676A1 - Méthode de production d'oxygène gazeux et installation cryogénique pour la mise en oeuvre de cette méthode - Google Patents

Méthode de production d'oxygène gazeux et installation cryogénique pour la mise en oeuvre de cette méthode Download PDF

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Publication number
EP0042676A1
EP0042676A1 EP81302417A EP81302417A EP0042676A1 EP 0042676 A1 EP0042676 A1 EP 0042676A1 EP 81302417 A EP81302417 A EP 81302417A EP 81302417 A EP81302417 A EP 81302417A EP 0042676 A1 EP0042676 A1 EP 0042676A1
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EP
European Patent Office
Prior art keywords
heat exchanger
stream
pressure column
sub
conduit
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.)
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Application number
EP81302417A
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German (de)
English (en)
Inventor
Alan Theobald
Brian Alfred Mcneil
Rodney John Allam
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Publication date
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Publication of EP0042676A1 publication Critical patent/EP0042676A1/fr
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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
    • F25J3/04006—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
    • F25J3/04151—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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • 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

Definitions

  • This invention relates to a method for producing gaseous oxygen and to a cryogenic plant in which said method can be carried out.
  • the nitrogen rich gas is preferably taken from the top of the high pressure column where it is substantially pure. This enables a substantially pure stream of nitrogen to be drawn off the plant at an elevated pressure if desired.
  • the first sub-stream and the second sub-stream may be compressed to the same pressure although normally the first sub-stream will be compressed to a pressure 7 to 40 bars above the second sub-stream.
  • fluid leaving the expander to contain up to 15 mole percent liquid and preferably between 8 and 10 mole percent liquid.
  • the liquid is preferably separated from the gas and the liquid returned to the high pressure column as additional reflux.
  • the pressure of the first sub-stream will be between 40 and 80 bars absolute whilst the pressure of the second sub-stream will be between 30 and 50 bars absolute.
  • the present invention also provides a cryogenic plant for producing gaseous oxygen, which plant comprises a high pressure column and a low pressure column for distilling air, a heat exchanger in which liquid oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the bottom of said low pressure column and introducing it into said heat exchanger, a compressor, a conduit for carrying nitrogen rich gas from said high pressure column to said compressor, a conduit for conveying a first sub-stream of compressed nitrogen rich gas from said compressor through said heat exchanger in countercurrent flow to said liquid oxygen, an expansion valve for, in use, expanding cold nitrogen rich gas leaving said heat exchanger and a conduit for conveying liquified nitrogen rich gas from said expansion valve to said high pressure column, characterized in that a further conduit is provided for conveying a second sub-stream of compressed nitrogen rich gas from said compressor to said heat exchanger to cool said compressed nitrogen rich gas, an expander for allowing compressed nitrogen rich gas from said heat exchanger to'expand, a conduit for conveying nitrogen rich gas from said expander to said heat exchanger
  • a cryogenic plant for producing gaseous oxygen which plant comprises a high pressure column and a low pressure column for distilling air, a heat exchanger in which liquid oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the bottom of said low pressure column and introducing it into said heat exchanger, a compressor, a conduit for carrying substantially pure gaseous nitrogen from the top of said high pressure column to said compressor, a conduit for conveying a first sub-stream of substantially pure compressed nitrogen from said compressor through said heat exchanger in countercurrent flow to said liquid oxygen, an expansion valve for, in use, expanding substantially pure cold nitrogen leaving said heat exchanger and a conduit for conveying substantially pure liquid nitrogen from said expansion valve to said high pressure column, characterized in that a further conduit is provided for conveying a second sub-stream of substantially pure compressed nitrogen from said compressor to said heat exchanger to cool said compressed nitrogen, an expander for allowing substantially pure compressed nitrogen from said heat exchanger to expand, a conduit for conveying substantially pure gaseous nitrogen from said expander to said heat exchanger to assist
  • the present invention further provides a cryogenic plant for producing gaseous oxygen which plant comprises a high pressure column and a low pressure column for distilling air, a first heat exchanger in which liquid oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the bottom of said low pressure column and introducing it into said first heat exchanger, a compressor, a conduit for carrying nitrogen rich gas from said high pressure column to said compressor, a conduit for conveying a first sub-stream of compressed nitrogen rich gas from said compressor through said first heat exchanger in countercurrent flow to said liquid oxygen, an expansion valve for, in use, expanding cold nitrogen rich gas leaving said heat exchanger and a conduit for conveying liquified nitrogen rich gas from said expansion valve to said high pressure column, characterized in that a further conduit is provided for conveying a second sub-stream of compressed nitrogen rich gas from said compressor to a second heat exchanger to cool said compressed nitrogen rich gas, an expander for allowing compressed nitrogen rich gas from said second heat exchanger to expand, a conduit for conveying nitrogen rich gas from said expander to said first
  • cryogenic plant for producing gaseous oxygen which plant comprises a high pressure column and a low pressure column for distilling air, a first heat exchanger in which liquid oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the bottom of said low pressure column and introducing it into said first heat exchanger, a compressor, a conduit for carrying substantially pure gaseous nitrogen from the top of said high pressure column to said compressor, a conduit for conveying a first sub-stream of substantially pure compressed nitrogen from said compressor through said first heat exchanger in countercurrent flow to said liquid oxygen, an expansion valve for, in use, expanding substantially pure cold nitrogen leaving said heat exchanger and a conduit for conveying substantially pure liquid nitrogen from said expansion valve to said high pressure column, characterized in that further conduit is provided for conveying a second sub-stream of substantially pure compressed nitrogen from said compressor to a second heat exchanger to cool said substantially pure compressed nitrogen, an expander for allowing substantially pure compressed nitrogen from said second heat exchanger to expand, a conduit for conveying substantially pure gaseous nitrogen from said expander to said
  • the first heat exchanger is a wound coil heat exchanger and the second heat exchanger is a plate-fin heat exchanger.
  • air at a flowrate of 5934 Kg moles/hour is compressed to 6.5 bars absolute (bars A) in compressor 1 and is subsequently passed through molecular sieve adsorbers 2 where water, carbon dioxide and any heavy hydrocarbons present are adsorbed.
  • the air leaves the molecular sieve adsorbers 2 through conduit 3 at 6.1 bars A and 10°C. It is then cooled to -172 C in heat exchanger 4 which it leaves through conduit 5 at a condition close to saturation.
  • the stream in conduit 5 is then introduced into the high pressure column 6 of a double column 7.
  • a crude liquid oxygen stream is withdrawn from the bottom of the high pressure column 6 through conduit 8 and after being subcooled to -177°C in subcooler 9 is expanded to 1.5 bars A at valve 10 and introduced into low pressure column 11 which is provided with a reboiler 12.
  • Liquid oxygen at 98 molar % purity accumulates in the bottom of the low pressure column 11 and passes to the inlet of pump 13 through conduit 14.
  • the liquid is then pumped at a rate of 1162 Kg moles/hour to heat exchanger 15 where it vaporizes and leaves through conduit 16 at 69 bars A and 20°C to form the gaseous oxygen product stream.
  • Gaseous nitrogen is withdrawn from the top of the high pressure column 6 through conduit 17. A portion of this nitrogen is condensed in reboiler 12 and returned to the high pressure column 6 through conduit 18 and the remainder through conduit 19 and sub-cooler 9 to product at the rate of 17 kg. moles/hour.
  • the remaining nitrogen in conduit 17 passes through conduit 20. It is joined at junction 21 by nitrogen from conduit 22 and the combined stream is passed through conduit 23 to heat exchanger 4. After being warmed to -125 o C, a portion of the nitrogen is withdrawn through conduit 24 and the balance leaves the heat exchanger 4 through conduit 25 at 6°C. It is joined by nitrogen from conduit 26 at junction 27 and the combined stream is introduced into the first stage 28 of a compressor 29.
  • the nitrogen is compressed to 41 bars A and leaves the first stage 28 through conduit 30.
  • a second sub-stream 31 is then withdrawn and the balance is compressed to 61 bars A in second stage 32 and product nitrogen at a flowrate of 1367 Kg moles/hour is withdrawn through conduit 33.
  • the remaining nitrogen is compressed to 80 bars A in the third stage 34 of compressor 29 which is leaves through conduit 35 as a first sub-stream.
  • the first sub-stream is cooled to -169°C in heat exchanger 15 which it leaves as a sub-cooled vapour as it is above its critical pressure. It is then expanded to 5.9 bars A at valve 36 and the two phases thus formed are separated in phase separator 37.
  • Liquid nitrogen is withdrawn from the bottom of the phase separator 37 and is returned to the high pressure column 6 through conduit 39 as reflux.
  • the nitrogen at 41 bars A is cooled to -123°C in heat exchanger 15 and is then expanded through generator loaded expander 40 to 5.9 bars A.
  • the two phase nitrogen leaving the expander 40 through conduit 41 contains 8 mole percent liquid and is introduced into phase separator 37.
  • the gaseous nitrogen in the phase separator 37 passes to junction 42.
  • Gaseous nitrogen is passed through conduit 22 to junction 21 whilst the balance is introduced into the cold end of heat exchanger 15 through conduit 43.
  • the nitrogen After being warmed to -125°C the nitrogen is joined by nitrogen from conduit 24 at junction 44.
  • the combined stream is then warmed and enters conduit 26.
  • a nitrogen-rich liquid fraction is taken from the high pressure column 6 through conduit 44 to sub-cooler 9 which it leaves through conduit 45. It is then expanded at valve 46 and the resulting two phase mixture is introduced into the low pressure column 11. Waste nitrogen leaves the top of the low pressure column 11 through conduit 47 and after being warmed in sub-cooler 9, enters heat exchanger 4 via conduit 47. The waste nitrogen leaves heat exchanger 4 through conduit 48 and a portion is used for regenerating the molecular sieves 2. The remainder is vented to atmosphere through conduit 49.
  • heat exchangers 4 and 15 will normally be plate-fin heat exchangers where pressure permit, it may be necessary for heat exchanger 15 to be a wound coil heat exchanger (generally where the pressure of the oxygen stream exceeds 81 bars A).
  • wound coil heat exchangers are relatively expensive, it may be desirable to use a plate-fin heat exchanger in combination with a wound coil heat exchanger in place of a single wound coil heat exchanger 15.
  • FIG. 2 shows a cryogenic plant which is generally similar to that shown in Figure 1 except that the liquid oxygen is pumped to 98 bars A by pump 13.
  • the second and third stages of the compressor have been combined into a single second stage 51 which compresses the nitrogen to 74 bars A.
  • the heat exchanger 15 is of the wound coil type. Because of the cost and complexity of building a wound coil heat exchanger with the flows arranged as shown in Figure 1, the second sub-stream 31 is cooled in a separate plate-fin heat exchanger 52 before being expanded as before. Cooling of the second sub-stream is effected by a stream 53 taken from conduit 24, passed through plate-fin heat exchanger 52 and returned to conduit 26 as shown.
  • heat exchanger 4 may be replaced with a reversing heat exchanger the and molecular sieve adsorbers omitted. In such an embodiment it will be necessary to place a hydrocarbon absorber in conduit 8 downstream of subcooler 9.
  • the second stage 32 and/or third stages 34 of the compressor 29 could be separate and distinct from the first stage 28 and driven, for example completely, or in part, by expander 40.
EP81302417A 1980-06-17 1981-06-02 Méthode de production d'oxygène gazeux et installation cryogénique pour la mise en oeuvre de cette méthode Withdrawn EP0042676A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
GB8019739 1980-06-17
GB8019739 1980-06-17
GB8037913A GB2079428A (en) 1980-06-17 1980-11-26 A method for producing gaseous oxygen
GB8037913 1980-11-26

Publications (1)

Publication Number Publication Date
EP0042676A1 true EP0042676A1 (fr) 1981-12-30

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EP81302417A Withdrawn EP0042676A1 (fr) 1980-06-17 1981-06-02 Méthode de production d'oxygène gazeux et installation cryogénique pour la mise en oeuvre de cette méthode

Country Status (5)

Country Link
EP (1) EP0042676A1 (fr)
AU (1) AU7146481A (fr)
ES (2) ES503090A0 (fr)
GB (1) GB2079428A (fr)
IL (1) IL63069A0 (fr)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2192265A (en) * 1986-05-21 1988-01-06 Dowty Fuel Syst Ltd Cooling systems
EP0504029A1 (fr) * 1991-03-11 1992-09-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de production d'oxygène gazeux sous pression
FR2674011A1 (fr) * 1991-03-11 1992-09-18 Grenier Maurice Procede et installation de production d'oxygene gazeux sous pression.
FR2681415A1 (fr) * 1991-09-18 1993-03-19 Air Liquide Procede et installation de production d'oxygene gazeux sous haute pression par distillation d'air.
EP0538118A1 (fr) * 1991-10-15 1993-04-21 Liquid Air Engineering Corporation Procédé de destillation cryogénique pour la production de l'oxygène et de l'azote
EP0540901A1 (fr) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Système de rectification cryogénique à récupération d'oxygène améliorée
EP0562893A1 (fr) * 1992-03-24 1993-09-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de production d'azote sous haute pression et d'oxygène
EP0567098A1 (fr) * 1992-04-22 1993-10-27 Praxair Technology, Inc. Système de rectification cryogénique à double pompe à chaleur
EP0713069A1 (fr) * 1991-12-18 1996-05-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de séparation d'air
EP0766054A2 (fr) † 1995-09-29 1997-04-02 Praxair Technology, Inc. Système de rectification cryogénique avec expansion à turbo à double phase
FR2778971A1 (fr) * 1998-05-20 1999-11-26 Air Liquide Installation de production d'un gaz, forme d'un constituant ou d'un melange de constituants de l'air sous une haute pression
WO2012019753A3 (fr) * 2010-08-13 2013-01-24 Linde Aktiengesellschaft Procédé et dispositif permettant d'obtenir de l'oxygène sous pression et de l'azote sous pression par fractionnement cryogénique de l'air
CN107131718A (zh) * 2015-12-07 2017-09-05 林德股份公司 在空气分离设备中获得液态和气态富氧空气产品的方法及空气分离设备
US20180073804A1 (en) * 2016-08-30 2018-03-15 8 Rivers Capital, Llc Cryogenic air separation method for producing oxygen at high pressures
FR3058785A1 (fr) * 2016-11-17 2018-05-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de separation d’air par distillation cryogenique mettant en oeuvre la detente d’un gaz

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3083544A (en) * 1958-09-24 1963-04-02 Linde S Eismaschinen Ag Hollri Rectification of gases
US3605422A (en) * 1968-02-28 1971-09-20 Air Prod & Chem Low temperature frocess for the separation of gaseous mixtures
EP0024962A1 (fr) * 1979-07-20 1981-03-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression
EP0029656A1 (fr) * 1979-10-23 1981-06-03 Air Products And Chemicals, Inc. Procédé et installation cryogénique pour la production de l'oxygène gazeux

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3083544A (en) * 1958-09-24 1963-04-02 Linde S Eismaschinen Ag Hollri Rectification of gases
US3605422A (en) * 1968-02-28 1971-09-20 Air Prod & Chem Low temperature frocess for the separation of gaseous mixtures
EP0024962A1 (fr) * 1979-07-20 1981-03-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression
EP0029656A1 (fr) * 1979-10-23 1981-06-03 Air Products And Chemicals, Inc. Procédé et installation cryogénique pour la production de l'oxygène gazeux

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2192265A (en) * 1986-05-21 1988-01-06 Dowty Fuel Syst Ltd Cooling systems
US5329776A (en) * 1991-03-11 1994-07-19 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the production of gaseous oxygen under pressure
EP0504029A1 (fr) * 1991-03-11 1992-09-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de production d'oxygène gazeux sous pression
FR2674011A1 (fr) * 1991-03-11 1992-09-18 Grenier Maurice Procede et installation de production d'oxygene gazeux sous pression.
FR2681415A1 (fr) * 1991-09-18 1993-03-19 Air Liquide Procede et installation de production d'oxygene gazeux sous haute pression par distillation d'air.
US5337571A (en) * 1991-09-18 1994-08-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen gas under high pressure by air distillation
EP0540901A1 (fr) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Système de rectification cryogénique à récupération d'oxygène améliorée
EP0538118A1 (fr) * 1991-10-15 1993-04-21 Liquid Air Engineering Corporation Procédé de destillation cryogénique pour la production de l'oxygène et de l'azote
US5231837A (en) * 1991-10-15 1993-08-03 Liquid Air Engineering Corporation Cryogenic distillation process for the production of oxygen and nitrogen
EP0713069A1 (fr) * 1991-12-18 1996-05-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de séparation d'air
US5341647A (en) * 1992-03-24 1994-08-30 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Porcess and apparatus for the production of high pressure nitrogen and oxygen
FR2689224A1 (fr) * 1992-03-24 1993-10-01 Air Liquide Procédé et installation de production d'azote sous haute pression et d'oxygène.
EP0562893A1 (fr) * 1992-03-24 1993-09-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de production d'azote sous haute pression et d'oxygène
EP0567098A1 (fr) * 1992-04-22 1993-10-27 Praxair Technology, Inc. Système de rectification cryogénique à double pompe à chaleur
EP0766054A2 (fr) † 1995-09-29 1997-04-02 Praxair Technology, Inc. Système de rectification cryogénique avec expansion à turbo à double phase
EP0766054B2 (fr) † 1995-09-29 2004-08-18 Praxair Technology, Inc. Système de rectification cryogénique avec expansion à turbo à double phase
FR2778971A1 (fr) * 1998-05-20 1999-11-26 Air Liquide Installation de production d'un gaz, forme d'un constituant ou d'un melange de constituants de l'air sous une haute pression
WO2012019753A3 (fr) * 2010-08-13 2013-01-24 Linde Aktiengesellschaft Procédé et dispositif permettant d'obtenir de l'oxygène sous pression et de l'azote sous pression par fractionnement cryogénique de l'air
CN103069238A (zh) * 2010-08-13 2013-04-24 林德股份公司 通过空气的低温分离获得压缩氧和压缩氮的方法和装置
US9733014B2 (en) 2010-08-13 2017-08-15 Linde Aktiengesellschaft Method and device for obtaining compressed oxygen and compressed nitrogen by the low-temperature separation of air
CN107131718A (zh) * 2015-12-07 2017-09-05 林德股份公司 在空气分离设备中获得液态和气态富氧空气产品的方法及空气分离设备
CN107131718B (zh) * 2015-12-07 2020-12-22 林德股份公司 在空气分离设备中获得液态和气态富氧空气产品的方法及空气分离设备
US20180073804A1 (en) * 2016-08-30 2018-03-15 8 Rivers Capital, Llc Cryogenic air separation method for producing oxygen at high pressures
US10746461B2 (en) * 2016-08-30 2020-08-18 8 Rivers Capital, Llc Cryogenic air separation method for producing oxygen at high pressures
FR3058785A1 (fr) * 2016-11-17 2018-05-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de separation d’air par distillation cryogenique mettant en oeuvre la detente d’un gaz

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IL63069A0 (en) 1981-09-13
ES512481A0 (es) 1983-02-01
ES8306070A1 (es) 1982-10-01
GB2079428A (en) 1982-01-20
AU7146481A (en) 1981-12-24
ES503090A0 (es) 1982-10-01

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