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EP0677713A1 - Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Tieftemperaturverlegung von Luft - Google Patents

Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Tieftemperaturverlegung von Luft Download PDF

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Publication number
EP0677713A1
EP0677713A1 EP95400752A EP95400752A EP0677713A1 EP 0677713 A1 EP0677713 A1 EP 0677713A1 EP 95400752 A EP95400752 A EP 95400752A EP 95400752 A EP95400752 A EP 95400752A EP 0677713 A1 EP0677713 A1 EP 0677713A1
Authority
EP
European Patent Office
Prior art keywords
pressure column
low pressure
column
air
level
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.)
Granted
Application number
EP95400752A
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English (en)
French (fr)
Other versions
EP0677713B1 (de
Inventor
Yves Koeberle
Philippe Fraysse
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
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
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0677713A1 publication Critical patent/EP0677713A1/de
Application granted granted Critical
Publication of EP0677713B1 publication Critical patent/EP0677713B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • F25J3/04006—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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • 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
    • F25J3/04248—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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • 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
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/92—Details relating to the feed point
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/58—Argon
    • 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 present invention relates to a method and an installation for the production of oxygen by air distillation and more particularly to a method and an installation for the production of oxygen under pressure.
  • EP-A-422,974 describes a process for the production of oxygen under pressure by cryogenic distillation of air in a double column. Liquid oxygen is withdrawn from the tank of the low pressure column 7, as illustrated in FIG. 1, and is vaporized in the auxiliary exchanger 9 by heat exchange with a fraction of the supply air. The remaining part of the supply air is divided into two flows, one of which goes directly to the medium pressure column 6, via line 14, and the other of which is expanded in a turbine 4 before being sent at the low pressure column 7.
  • a first object of this invention is to reduce the costs of the energy used by a process for producing pressurized oxygen compared to those of known processes.
  • a second object of this invention is to improve the argon yields in the case where the installation also includes an argon column supplied by the low pressure column.
  • the subject of the invention is a process for the production of gaseous oxygen under pressure by cryogenic distillation of air in a double column comprising a medium pressure column and a low pressure column, in which the rich liquid from the medium pressure column in first and second liquid fractions which are sent to different levels in the low pressure column, characterized in that the different levels are below a level of drawing off impure nitrogen from the column low pressure.
  • the rich liquid of the medium pressure column is divided into first and second fractions and the first and second fractions are sent to different levels in the low pressure column after sub-cooling. prior. This notably makes it possible to substantially improve the extraction of argon in the case where the installation also comprises an argon column.
  • the two fractions can be sent to the low pressure column at different temperatures, in order to further improve the reflux in the low pressure column and the extraction of argon in the case where the installation also includes an argon column.
  • part of the supply air is expanded before being sent to the double column, the remaining part of the supply air being partially condensed in the auxiliary exchanger.
  • the temperature difference in the auxiliary exchanger can be reduced to an average value of 0.6 ° C.
  • the invention also relates to an installation for producing gaseous oxygen under pressure by cryogenic distillation of air comprising a double column, consisting of at least one medium pressure column surmounted by a column of a low pressure column, means for withdrawing impure nitrogen from the low pressure column, and means for withdrawing rich liquid from the tank of the medium pressure column and sending it to two different levels of the low pressure column, located below the withdrawal level impure nitrogen.
  • the installation shown in FIG. 1 essentially comprises a main air compressor 1 with variable flow rate, for example of the centrifugal type with moving blades, an air blower with moving blades 2, a heat exchange line 3, a turbine 4 for keeping cold, an air distillation apparatus 5 constituted by a double column itself comprising a medium pressure column 6 surmounted by a low pressure column 7 and a minaret 7A, a vaporizer-condenser 8, a heat exchanger auxiliary heat 9 and a pump 10.
  • This installation is intended to produce a variable flow of gaseous oxygen via a line 12, under a pressure greater than atmospheric pressure.
  • the nominal flow of air to be treated, compressed to 6 bar by compressor 1, cooled to room temperature and purified, is divided into two fractions.
  • the first fraction is boosted by the booster 2 and the second fraction goes directly to the exchange line 3 where it is divided into two flows, each having a constant flow: -
  • a first flow is cooled in passages of the exchange line; a portion has left this exchange line after partial cooling, expanded to 1 bar in the turbine 4 and blown into the low pressure column 7 near its dew point; a second flow continues to cool down to the vicinity of its dew point under 6 bar, then is injected at the bottom of the medium pressure column 6 via a pipe 14.
  • the first overpressed fraction is cooled to the vicinity of its dew point in passages of the exchange line and then condensed in the auxiliary exchanger 9 and is divided into a first constant flow expanded under 6 bar sent to the medium pressure column. via a line 16, and a second constant flow expanded to around 1 bar in an expansion valve 13 then injected into the low pressure column 7.
  • the vaporizer-condenser 8 vaporizes a constant flow of liquid oxygen in the bottom of the low pressure column by condensing a roughly equal flow of nitrogen from the top of the medium pressure column.
  • "Rich liquid” oxygen-enriched air
  • "lean liquid” nitrogen approximately pure taken at the head of the medium pressure column and expanded to around 1 bar in an expansion valve 19 is injected at the top of the low pressure column.
  • Liquid nitrogen is injected at the top of the minaret 7A through the expansion valve 21. Pure nitrogen is withdrawn from the top of the minaret 7A and sent to the exchange line 3 to be reheated before coming out through the line 20. The impure nitrogen leaves via line 25 from the top of the low pressure column 7 and is sent to the outside via line 18.
  • Liquid oxygen withdrawn from the tank of the low pressure column 7 is pumped to production pressure before being vaporized in the auxiliary exchanger 9 (constituted by a "film” type vaporizer) by heat exchange with the air that partially condenses there.
  • the vaporized oxygen leaves, after heating in the exchange line 3, via line 12.
  • an argon-rich fraction is drawn from the lower part of the low pressure column 7 and is sent to the argon column 16 for distillation.
  • This fraction mainly comprises argon and oxygen.
  • the tank liquid resulting from the distillation in column 16 is returned to the lower part of the low pressure column 7.
  • the overhead condenser 29 of the argon column 16 is cooled by rich liquid coming from the tank of the medium pressure column 6 , expanded by valve 23, vaporized and sent to the low pressure column.
  • the remaining part of the rich liquid from the tank of the medium pressure column 6 is expanded by the valve 18 to a pressure slightly above atmospheric pressure and sent into the low pressure column 7 by the valve 18, substantially at the same level as the injection level of the air expanded by the turbine 4 (the blowing air).
  • the installation shown in FIG. 2 differs from the prior art in that all the air which is not overpressed by the booster 2 is sent to the turbine 4 to be expanded and sent to the low pressure column 7.
  • the pressurized and partially condensed air in the auxiliary exchanger 9 is entirely injected into the tank of the medium pressure column 6.
  • the remaining part of rich liquid not vaporized at 29 is divided into two fractions: a first fraction is injected, as shown in FIG. 1, after expansion by the valve 18 in the low pressure column 7 at the level of the air supply and the second fraction of rich liquid is sent to the low pressure column 7, after expansion to the pressure of the latter by the valve 17, at an intermediate level between the level of injection of the first fraction of rich liquid through the valve 18 and the level of withdrawal of nitrogen through the line 25.
  • FIG. 3 has only one air compressor 1, all the compressed air being sent either to the turbine 4 or to the exchanger 9.
  • the partially condensed air in the exchanger 9 passes entirely to the tank of the medium pressure column 6.
  • the difference in level between the level of liquid oxygen in the tank of the LP column and its entry into the vaporizer 9 fixes, in this case, the vaporization pressure of the oxygen; the pump 10 in Figure 2 is therefore deleted.
  • the fractions of rich liquid can be sub-cooled so that the temperature of the fraction injected at the level of air blowing is lower than that of the fraction injected at the intermediate level.
  • This arrangement of the exchanger 9 allows a gain of about 6% on the compression of the air and therefore on the specific energy of the oxygen produced.

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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)
EP95400752A 1994-04-12 1995-04-04 Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Rektifikation von Luft Expired - Lifetime EP0677713B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9404298 1994-04-12
FR9404298A FR2718518B1 (fr) 1994-04-12 1994-04-12 Procédé et installation pour la production de l'oxygène par distillation de l'air.

Publications (2)

Publication Number Publication Date
EP0677713A1 true EP0677713A1 (de) 1995-10-18
EP0677713B1 EP0677713B1 (de) 1999-10-20

Family

ID=9461989

Family Applications (1)

Application Number Title Priority Date Filing Date
EP95400752A Expired - Lifetime EP0677713B1 (de) 1994-04-12 1995-04-04 Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Rektifikation von Luft

Country Status (7)

Country Link
US (1) US5586451A (de)
EP (1) EP0677713B1 (de)
JP (1) JPH0854181A (de)
CN (1) CN1121172A (de)
CA (1) CA2146831A1 (de)
DE (1) DE69512821T2 (de)
FR (1) FR2718518B1 (de)

Cited By (1)

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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

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GB9807833D0 (en) * 1998-04-09 1998-06-10 Boc Group Plc Separation of air
US6178775B1 (en) * 1998-10-30 2001-01-30 The Boc Group, Inc. Method and apparatus for separating air to produce an oxygen product
GB9910701D0 (en) 1999-05-07 1999-07-07 Boc Group Plc Separation of air
GB9925097D0 (en) * 1999-10-22 1999-12-22 Boc Group Plc Air separation
US6253576B1 (en) * 1999-11-09 2001-07-03 Air Products And Chemicals, Inc. Process for the production of intermediate pressure oxygen
EP1338856A3 (de) * 2002-01-31 2003-09-10 L'AIR LIQUIDE, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Verfahren und Vorrichtung zur Zerlegung von Luft durch Tieftemperaturdestillation
FR2864214B1 (fr) * 2003-12-22 2017-04-21 Air Liquide Appareil de separation d'air, appareil integre de separation d'air et de production d'un metal et procede de demarrage d'un tel appareil de separation d'air
US20070095100A1 (en) * 2005-11-03 2007-05-03 Rankin Peter J Cryogenic air separation process with excess turbine refrigeration
US9279613B2 (en) 2010-03-19 2016-03-08 Praxair Technology, Inc. Air separation method and apparatus
CN105115244B (zh) * 2015-08-10 2017-06-27 开封空分集团有限公司 一种低纯度氧空气分离的装置及方法

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FR1253717A (fr) * 1960-04-08 1961-02-10 Union Carbide Corp Séparation à basse température de l'air en oxygène, azote et argon
US3214925A (en) * 1960-08-13 1965-11-02 Linde Eismasch Ag System for gas separation by rectification at low temperatures
WO1988001037A1 (en) * 1986-08-01 1988-02-11 Erickson Donald C Air distillation improvements for high purity oxygen
EP0357299A1 (de) * 1988-08-31 1990-03-07 The BOC Group plc Lufttrennung
EP0454327A1 (de) * 1990-04-18 1991-10-30 The BOC Group plc Lufttrennung
US5228296A (en) * 1992-02-27 1993-07-20 Praxair Technology, Inc. Cryogenic rectification system with argon heat pump
EP0580348A1 (de) * 1992-07-20 1994-01-26 Air Products And Chemicals, Inc. Hybrider Luft und Stickstoff Kreislaufverflüssiger

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FR2655137B1 (fr) * 1989-11-28 1992-10-16 Air Liquide Procede et installation de distillation d'air avec production d'argon.
US4994098A (en) * 1990-02-02 1991-02-19 Air Products And Chemicals, Inc. Production of oxygen-lean argon from air
US5076823A (en) * 1990-03-20 1991-12-31 Air Products And Chemicals, Inc. Process for cryogenic air separation

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Publication number Priority date Publication date Assignee Title
FR1253717A (fr) * 1960-04-08 1961-02-10 Union Carbide Corp Séparation à basse température de l'air en oxygène, azote et argon
US3214925A (en) * 1960-08-13 1965-11-02 Linde Eismasch Ag System for gas separation by rectification at low temperatures
WO1988001037A1 (en) * 1986-08-01 1988-02-11 Erickson Donald C Air distillation improvements for high purity oxygen
EP0357299A1 (de) * 1988-08-31 1990-03-07 The BOC Group plc Lufttrennung
EP0454327A1 (de) * 1990-04-18 1991-10-30 The BOC Group plc Lufttrennung
US5228296A (en) * 1992-02-27 1993-07-20 Praxair Technology, Inc. Cryogenic rectification system with argon heat pump
EP0580348A1 (de) * 1992-07-20 1994-01-26 Air Products And Chemicals, Inc. Hybrider Luft und Stickstoff Kreislaufverflüssiger

Cited By (1)

* 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

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Publication number Publication date
JPH0854181A (ja) 1996-02-27
FR2718518B1 (fr) 1996-05-03
DE69512821D1 (de) 1999-11-25
CN1121172A (zh) 1996-04-24
US5586451A (en) 1996-12-24
DE69512821T2 (de) 2000-05-25
EP0677713B1 (de) 1999-10-20
FR2718518A1 (fr) 1995-10-13
CA2146831A1 (fr) 1995-10-13

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