EP1106945B1 - Verfahren zur Luftzerlegung durch Tieftemperaturdestillation - Google Patents

Verfahren zur Luftzerlegung durch Tieftemperaturdestillation Download PDF

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Publication number
EP1106945B1
EP1106945B1 EP00403354A EP00403354A EP1106945B1 EP 1106945 B1 EP1106945 B1 EP 1106945B1 EP 00403354 A EP00403354 A EP 00403354A EP 00403354 A EP00403354 A EP 00403354A EP 1106945 B1 EP1106945 B1 EP 1106945B1
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EP
European Patent Office
Prior art keywords
column
liquid
mixing
gas
process according
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Expired - Lifetime
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EP00403354A
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English (en)
French (fr)
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EP1106945A1 (de
Inventor
Jean Renaud Brugerolle
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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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
    • F25J3/04642—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
    • F25J3/04715—The auxiliary column system simultaneously produces 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
    • F25J3/0446—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 the heat generated by mixing two different phases
    • 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
    • F25J3/0446—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 the heat generated by mixing two different phases
    • F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon

Definitions

  • the present invention relates to a separation method and installation of air by cryogenic distillation.
  • it relates to a method of pure oxygen production using a mixing column and possibly Argon production using an argon column
  • EP-A-0269342 relates to the case in which the argon column is connected thermally with a mixing column so that the lead gas of the Argon column heats the mixing column.
  • US-A-5551258 discloses a method according to the preamble of claim 1 wherein a mixing column is fed at the top by a liquid containing 55% vol. of oxygen, the top gas of the mixing column then serving to heat the tank condenser of the low pressure column.
  • An object of the present invention is to increase the amount of gaseous oxygen pure (containing more than 99.5 mol% of oxygen) that can be produced by a double air separation column.
  • the overhead gas of the mixing column can be withdrawn at the top of the mixing column or at most five theoretical plates below the top of the mixing column.
  • Figure 1 The installation of Figure 1 comprises a double column 1 comprising a medium pressure column 3 and a low pressure column 5 connected between they by a vaporizer 7.
  • the vaporizer includes liquid vaporization passages and two independent series of heating passages for two different heating gases.
  • the low pressure column operates at between 1.4 and 2.7 bar and the column medium pressure operates at between 5 and 8 bar.
  • the argon column 9 is fed from a first level of the column low pressure 5. There is also a mixing column 11 that operates at a pressure between 1.9 bar and 3.7 bar.
  • An air flow 13 is sent to the column 3 and a blown air flow 14 is sent to column 5.
  • a liquid flow containing 40 mol%. of oxygen is drawn from the medium pressure column vessel 3: a part 17 of this liquid feeds the low pressure column 5 after expansion in a valve and a part 19 of the liquid is relaxed to between 1.7 and 2.2 bar absolute in a valve and sent to head condenser 21 of the argon column 9 where it vaporizes at least partially.
  • the vaporized liquid 23 is sent to the bottom of the mixing column.
  • the nitrogen at the top of the medium pressure column condenses at least partially in the vessel vaporizer 7 and the condensate is sent to the column medium pressure and / or the low pressure column.
  • a gas flow 41 containing at least 80 mol% of nitrogen is drawn off at the head of the medium pressure column as a product and constitutes 10 to 15% of supply air.
  • a nitrogen-enriched liquid flow rate containing less than 2 mol% of oxygen is sent from the medium pressure column to the top of the column low pressure.
  • a liquid flow 27 containing less than 5 mol% of nitrogen is drawn off in low pressure column vessel 5 below the gas withdrawal point 26 for the argon column 9.
  • the second liquid is withdrawn from the low pressure column at a level at least 5 theoretical plateaus below the injection point of the low pressure column (or the point of injection most low), possibly at least 10 theoretical plateaus below the point injecting the low pressure column (or the lowest point of injection) and / or at a level of about one-third theoretical plateaus of the low pressure column above the tank of the low pressure column.
  • This liquid is sent after pumping to between 1.9 and 3.7 bar at the head of the mixing column 11.
  • this flow 27 is mixed with the liquid of tank 29 of the argon column before being pressurized and sent to the column of mixed.
  • a gas flow 31 containing at most 5 mol% of nitrogen is sent from the head of the mixing column to the vaporizer 7 where it is condensed in separate passages from those in which the nitrogen of the column is condensed medium pressure in order to increase the reflux in a low pressure column.
  • this nitrogen can condense air or other fluid less volatile than medium pressure nitrogen, provided that it is condensed in another system condenser, normally above the vaporizer.
  • Part of the flow 31 may serve as an oxygen enriched product.
  • An intermediate liquid 33 of the mixing column containing 80 mol%. of oxygen is sent to the low pressure column 5.
  • the tank liquid 35 of the mixing column containing 65 mol%. of oxygen is sent to the low pressure column 5.
  • a flow 37 containing more than 99.5 mol%. of oxygen is drawn off in the tank of the low pressure column 5 either in gaseous form or under liquid form.
  • the low pressure column is fed from downwardly with lean liquid containing less than 1 mol% oxygen, the insufflation air 14, the non-vaporized rich liquid 45 of the head condenser of the argon column, the rich liquid 17, the liquid of the tank of the mixing column 35, the intermediate liquid of the mixing column 33 and the recondensed mixture 31 of the vaporizer 7.
  • the low pressure column contains at least 80 theoretical trays and preferably at least 90 theoretical plateaus.
  • Figure 2 differs from that of Figure 1 in that the column The mixture is tank-fed exclusively by a flow of air from possibly a turbine or booster (not shown). The steam of condenser 21 of the argon column is sent to the low pressure column just below the point of injection of the rich liquid 45.
  • the argon column can be removed entirely or can be reduced to a simple liquid vaporizer heated by a gas from the low pressure column (which amounts to a column argon without theoretical distillation trays).
  • the argon column and / or the low pressure column can be constructed in two sections as described in EP-A-0628777.
  • the second liquid 27 is withdrawn from the low pressure column at a level at least 5 theoretical plateaus below the liquid injection point rich 45 of the low pressure column, possibly at least 10 theoretical plates below the injection point of the low pressure column, and / or at a level of about a third of theoretical plateaux of the low pressure column above the tank of the low pressure column.
  • the second liquid 27 is drawn off, preferably, at a level between the low pressure column vessel 5 and the level of withdrawal of the feed 26 of the argon column 9, in the case where there is an argon column.
  • medium pressure and low pressure columns can be built side by side.
  • the frigories necessary for the apparatus can be provided by at least an inflation turbine and / or at least one Claude turbine and / or at least one nitrogen turbine.
  • the apparatus can produce liquids and / or gases.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (15)

  1. Verfahren zur Luftzerlegung durch Tieftemperaturdestillation zur Produktion von Sauerstoff mit einer Doppelkolonne (1), die Folgendes umfasst:
    eine Mitteldruckkolonne (3)
    eine Niederdruckkolonne (5), die einen Verdampfer (7) zum Verdampfen der Flüssigkeit im Sumpf der Niederdruckkolonne umfasst,
    das die folgenden Schritte umfasst:
    Senden von gekühlter und verdichteter Luft zur Mitteldruckkolonne,
    Senden einer mit Sauerstoff angereicherten Flüssigkeit und einer mit Stickstoff angereicherten Flüssigkeit von der Mitteldruckkolonne zu der Niederdruckkolonne,
    Senden von Gas (23) zum Sumpf der Mischkolonne (11),
    Senden einer zweiten mit Sauerstoff angereicherten Flüssigkeit (27) von der Niederdruckkolonne zum Kopf der Mischkolonne, wobei diese zweite Flüssigkeit weniger flüchtig als das dem Sumpf der Mischkolonne zugeführte Gas ist,
    Abziehen eines mit Sauerstoff angereicherten Fluids (37) aus der Niederdruckkolonne,
    Senden mindestens eines Teils eines Gases, eventuell des Gases im Kopf von der Mischkolonne zu den Durchlässen zum Erhitzen des Verdampfers,
    dadurch gekennzeichnet, dass die zweite Flüssigkeit mindestens 5 Mol-% Stickstoff enthält und das von der Mischkolonne zu den Heizdurchlässen gesendete Gas mit Sauerstoff angereichert ist und mindestens 15 Mol-% Stickstoff enthält.
  2. Verfahren nach Anspruch 1, in dem es sich beim zum Sumpf der Mischkolonne gesendeten Gas (23) um eine mit Sauerstoff angereicherte, verdampfte Flüssigkeit handelt, die in flüssiger Form (19) aus der Mitteldruckkolonne abgezogen und anschließend verdampft wurde.
  3. Verfahren nach Anspruch 2, in dem die Flüssigkeit in einem Kondensator im Kopf (21) einer Argonkolonne (9) verdampft wird.
  4. Verfahren nach Anspruch 2, in dem die Flüssigkeit in einem Kondensator verdampft wird, der mittels eines von der Niederdruckkolonne (5) stammenden Gases erhitzt wurde.
  5. Verfahren nach einem der Ansprüche 1 bis 4, in dem das Gas im Kopf der Mischkolonne (11) mindestens teilweise im Verdampfer (7) kondensiert und das Kondensat eventuell an eine Ebene über einer ersten Ebene der Niederdruckkolonne gesendet wird, von wo ein mit Argon angereichertes Gas abgezogen und in eine Argonkolonne gesendet wird.
  6. Verfahren nach Anspruch 3, das den Schritt des Sendens der Flüssigkeit vom Sumpf der Argonkolonne (9) zum Kopf der Mischkolonne (11) umfasst.
  7. Verfahren nach einem der Ansprüche 1 bis 6, das den Schritt des Sendens einer Flüssigkeit vom Sumpf und/oder einer Flüssigkeit vom Mittelteil der Mischkolonne (11) zu der Doppelkolonne (1) umfasst.
  8. Verfahren nach einem der Ansprüche 1 bis 7, in dem ein Gas in der Mitteldruckkolonne oder Luft mindestens teilweise in anderen Durchlässen zur Erhitzung des Verdampfers kondensiert.
  9. Verfahren nach einem der Ansprüche 1 bis 8, in dem das Gas im Kopf der Mischkolonne (11) 0,1 bis 5 Mol-% Stickstoff, vorzugsweise zwischen 1 und 3 Mol-% Stickstoff umfasst.
  10. Verfahren nach einem der Ansprüche 1 bis 9, in dem das Gas im Kopf der Mischkolonne (11) mindestens 93 Mol-%, eventuell mindestens 95 Mol-% Sauerstoff umfasst.
  11. Verfahren nach einem der Ansprüche 1 bis 10, in dem die zum Kopf der Mischkolonne (11) gesendete Flüssigkeit mindestens 99 Mol-% Sauerstoff enthält.
  12. Verfahren nach einem der Ansprüche 1 bis 11, in dem Luft zu einer Einblasturbine gesendet wird, die die Luft zu der Niederdruckkolonne oder der Mischkolonne (11) sendet.
  13. Verfahren nach einem der Ansprüche 1 bis 12, in dem das Gas vom Kopf der Mitteldruckkolonne als Produkt abgezogen wird.
  14. Verfahren nach einem der Ansprüche 1 bis 13, in dem das zum Sumpf der Mischkolonne gesendete Gas im Vergleich zu Luft mit Sauerstoff angereichert ist.
  15. Verfahren nach einem der Ansprüche 1 bis 14, in dem die Mischkolonne bei einem Druck zwischen 0,5 und 1 bar über dem Druck der Niederdruckkolonne betrieben wird.
EP00403354A 1999-12-02 2000-11-30 Verfahren zur Luftzerlegung durch Tieftemperaturdestillation Expired - Lifetime EP1106945B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9915208 1999-12-02
FR9915208A FR2801963B1 (fr) 1999-12-02 1999-12-02 Procede et installation de separation d'air par distillation cryogenique

Publications (2)

Publication Number Publication Date
EP1106945A1 EP1106945A1 (de) 2001-06-13
EP1106945B1 true EP1106945B1 (de) 2005-06-01

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EP00403354A Expired - Lifetime EP1106945B1 (de) 1999-12-02 2000-11-30 Verfahren zur Luftzerlegung durch Tieftemperaturdestillation

Country Status (6)

Country Link
US (1) US6385996B2 (de)
EP (1) EP1106945B1 (de)
JP (1) JP2001194058A (de)
AT (1) ATE297001T1 (de)
DE (1) DE60020500T2 (de)
FR (1) FR2801963B1 (de)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2854232A1 (fr) * 2003-04-23 2004-10-29 Air Liquide Procede de distillation d'air pour produire de l'argon
CN102620520B (zh) * 2012-04-09 2014-09-17 开封黄河空分集团有限公司 一种由空气分离制取压力氧气和压力氮气附产液氩的工艺
CN103162512B (zh) * 2013-01-27 2015-06-10 南京瑞柯徕姆环保科技有限公司 一种等压分离制取氧氮的空分装置
JP5655104B2 (ja) 2013-02-26 2015-01-14 大陽日酸株式会社 空気分離方法及び空気分離装置
EP3557166A1 (de) 2018-04-19 2019-10-23 Linde Aktiengesellschaft Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4022030A (en) 1971-02-01 1977-05-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Thermal cycle for the compression of a fluid by the expansion of another fluid
FR2584803B1 (fr) * 1985-07-15 1991-10-18 Air Liquide Procede et installation de distillation d'air
FR2655137B1 (fr) * 1989-11-28 1992-10-16 Air Liquide Procede et installation de distillation d'air avec production d'argon.
FR2680114B1 (fr) * 1991-08-07 1994-08-05 Lair Liquide Procede et installation de distillation d'air, et application a l'alimentation en gaz d'une acierie.
EP0636845B1 (de) * 1993-04-30 1999-07-28 The BOC Group plc Lufttrennung
US5379599A (en) 1993-08-23 1995-01-10 The Boc Group, Inc. Pumped liquid oxygen method and apparatus
US5490391A (en) * 1994-08-25 1996-02-13 The Boc Group, Inc. Method and apparatus for producing oxygen
US5551258A (en) * 1994-12-15 1996-09-03 The Boc Group Plc Air separation
FR2774159B1 (fr) * 1998-01-23 2000-03-17 Air Liquide Installation combinee d'un four et d'un appareil de distillation d'air et procede de mise en oeuvre
US5865041A (en) * 1998-05-01 1999-02-02 Air Products And Chemicals, Inc. Distillation process using a mixing column to produce at least two oxygen-rich gaseous streams having different oxygen purities
GB9902101D0 (en) * 1999-01-29 1999-03-24 Boc Group Plc Separation of air

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Publication number Publication date
EP1106945A1 (de) 2001-06-13
US6385996B2 (en) 2002-05-14
FR2801963A1 (fr) 2001-06-08
JP2001194058A (ja) 2001-07-17
FR2801963B1 (fr) 2002-03-29
DE60020500D1 (de) 2005-07-07
DE60020500T2 (de) 2006-03-23
ATE297001T1 (de) 2005-06-15
US20010003909A1 (en) 2001-06-21

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