EP0384213A2 - Procédé et dispositif de rectification d'air - Google Patents

Procédé et dispositif de rectification d'air Download PDF

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Publication number
EP0384213A2
EP0384213A2 EP90102355A EP90102355A EP0384213A2 EP 0384213 A2 EP0384213 A2 EP 0384213A2 EP 90102355 A EP90102355 A EP 90102355A EP 90102355 A EP90102355 A EP 90102355A EP 0384213 A2 EP0384213 A2 EP 0384213A2
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EP
European Patent Office
Prior art keywords
rectification
medium pressure
pressure stage
oxygen
crude argon
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
EP90102355A
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German (de)
English (en)
Other versions
EP0384213A3 (en
EP0384213B1 (fr
Inventor
Dietrich Dipl.-Ing. Rottmann
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.)
Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Priority claimed from DE19893905521 external-priority patent/DE3905521A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP0384213A2 publication Critical patent/EP0384213A2/fr
Publication of EP0384213A3 publication Critical patent/EP0384213A3/de
Application granted granted Critical
Publication of EP0384213B1 publication Critical patent/EP0384213B1/fr
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
    • F25J3/04642—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
    • 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
    • F25J3/0423—Subcooling of liquid process streams
    • 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
    • F25J3/04327—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 argon or argon enriched 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
    • 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
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen enriched compared to air, e.g. "crude 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude 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
    • 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
    • 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 invention relates to a process for air separation by rectification, in which air is compressed, pre-cleaned, cooled and pre-separated into a nitrogen-rich fraction and an oxygen-rich liquid in the pressure stage of a two-stage rectification, and the two fractions are at least partially fed to the medium pressure stage of the rectification and in Oxygen and nitrogen are broken down and in which an argon-containing oxygen stream is taken from the medium pressure stage and fed to crude argon rectification, and also a device for carrying out the method.
  • the crude argon rectification is carried out under the pressure under which the argon-containing oxygen fraction is removed from the medium pressure stage. Liquid oxygen is recycled from crude argon rectification to approximately the same point in the medium pressure stage.
  • Such a method is favorable if the medium pressure stage and thus the crude argon rectification are carried out essentially under atmospheric pressure.
  • oxygen and / or nitrogen, which are generated in the medium pressure stage are required under increased pressure, for example in coal gasification plants or for blowing nitrogen in during the extraction of oil or natural gas. It is economically more advantageous for the production of pressurized nitrogen and oxygen to operate the medium pressure stage under an increased pressure, approximately 2.0 to 8.0 bar, than to subsequently compress products obtained without pressure.
  • the object on which the invention is based is to improve the method and the device of the type mentioned at the outset in such a way that both the production of pressurized nitrogen and pressurized oxygen and the production of argon can be carried out economically.
  • This object is achieved in that the crude argon rectification is operated under a pressure which is lower than the pressure of the medium pressure stage.
  • the pressure conditions in the crude argon rectification are no longer tied to those of the medium pressure stage, so that an optimal value for the argon yield of 1.1 to 2.0 bar, preferably 1.3 to 1.5 bar can be maintained. Nevertheless, the medium pressure stage can still release oxygen and nitrogen under increased pressure.
  • the argon-containing oxygen stream is expanded while performing work before being introduced into the crude argon rectification.
  • the energy recovered during expansion can be used to compress other process streams.
  • a lot of cold is generated during relaxation work, which is required for air separation. In this way, the supply of externally generated cold can be dispensed with at least in part.
  • the generally liquid residual fraction of crude argon rectification consists essentially of oxygen. Since it would be uneconomical to discard this fraction, it is proposed according to a further feature of the invention to return the liquid fraction from the crude argon rectification to the medium pressure stage and to pump it to the pressure of the medium pressure stage before introduction into the medium pressure stage.
  • the resulting vaporized oxygen-rich fraction is advantageously returned to the medium pressure stage.
  • the vaporized oxygen-rich fraction must be compressed in the medium pressure stage before being introduced.
  • the work obtained in the work-relieving expansion of the argon-containing oxygen stream is used at least in part to compress the vaporized oxygen-rich fraction.
  • the invention further relates to a device for carrying out the method according to claims 10 to 12.
  • Compressed and pre-cleaned air is supplied via line 1, cooled in a heat exchanger 36 in indirect heat exchange with product streams and fed into the pressure stage 3 of a two-stage rectification column 2.
  • the pressure level 3 (operating pressure: 6 to 20 bar, preferably 8 to 17 bar) is with the medium pressure level 4 (operating pressure: 1.5 to 10 bar, preferably 2.0 to 8.0 bar) via a common condenser / evaporator 13 in heat exchanging connection.
  • the introduced air is pre-divided in pressure stage 3 into nitrogen and into an oxygen-enriched fraction.
  • the oxygen-enriched fraction is discharged in the liquid state via line 6, subcooled in heat exchanger 32 and in part throttled via line 10 into the medium pressure stage 4.
  • Nitrogen from the head of pressure stage 3 is also drawn off in liquid form via line 5, subcooled in heat exchanger 32 and partly discharged as a liquid product via line 8.
  • the other part of the nitrogen from the pressure stage 3 is fed via line 9 as a return to the medium pressure stage 4.
  • liquid oxygen (line 14), gaseous pure nitrogen (line 15) and impure nitrogen (line 16) are removed and the nitrogen streams in the heat exchanger 32 are additionally heated.
  • an argon-containing oxygen stream is also removed from line 17 via line 17, heated in heat exchanger 36 and introduced into crude argon rectification 20, which is under a pressure of 1.1 bar to 2.0 bar, preferably 1.3 to 1.5 bar is operated.
  • the residual fraction obtained in the bottom of the crude argon rectification 20 is discharged via line 22 and brought according to the invention by pump 23 to the pressure required for feeding back into the medium pressure stage 4.
  • the argon-rich oxygen stream 17 is expanded prior to introduction into the crude argon rectification 20 in an expansion turbine 18 in order to bring it to the lower pressure prevailing in the crude argon rectification 20 on the one hand and to produce process cold on the other.
  • the gaseous crude argon obtained at the top of the crude argon rectification 20 is introduced via line 33 into a condenser 35, partly liquefied and partly returned via line 34 as a return to the crude argon rectification 20, partly discharged via line 21 as an intermediate product and heated in the heat exchanger 36 .
  • the condenser 35 is cooled by a portion of the oxygen-rich fraction 6 from the pressure stage, which is brought in via line 11, subcooled in a heat exchanger 24 and passed to the condenser 35 via line 25.
  • the portion evaporated during the indirect heat exchange with the top gas of the crude argon rectification 20 is discharged via line 26 and heated in the heat exchangers 24 and 36.
  • the oxygen-rich stream is compressed in two compressor stages 27 and 29 and then each cooled (water coolers 28 and 30).
  • the oxygen-rich stream is then passed via line 31 through the heat exchanger 36, cooled there again and then fed into the medium pressure stage 4. It is advantageous to use the work obtained in the expansion of the argon-rich oxygen fraction 17 to drive the compression 29.
  • part of the air in line 1 can be condensed in heat exchange with oxygen from the sump of medium pressure stage 4.
  • the liquid from the sump of the medium pressure stage can be brought to high pressure by means of a pump and partially evaporates during the heat exchange.
  • the partially condensed air is then introduced into the pressure stage 3 above the first feed point (line 1) shown in the drawing. This part of the process is not shown in the drawing, but can be economically advantageous at the indicated rectification pressures.

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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)
EP90102355A 1989-02-23 1990-02-07 Procédé et dispositif de rectification d'air Expired - Lifetime EP0384213B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19893905521 DE3905521A1 (de) 1989-02-23 1989-02-23 Verfahren und vorrichtung zur luftzerlegung durch rektifikation
DE3905521 1989-02-23
US07/483,142 US5034043A (en) 1989-02-23 1990-02-22 Air separation with argon recovery

Publications (3)

Publication Number Publication Date
EP0384213A2 true EP0384213A2 (fr) 1990-08-29
EP0384213A3 EP0384213A3 (en) 1990-10-24
EP0384213B1 EP0384213B1 (fr) 1992-12-02

Family

ID=47087703

Family Applications (1)

Application Number Title Priority Date Filing Date
EP90102355A Expired - Lifetime EP0384213B1 (fr) 1989-02-23 1990-02-07 Procédé et dispositif de rectification d'air

Country Status (6)

Country Link
US (1) US5034043A (fr)
EP (1) EP0384213B1 (fr)
JP (1) JPH02247485A (fr)
CN (1) CN1025067C (fr)
DE (1) DE59000514D1 (fr)
ZA (1) ZA901345B (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0527501A1 (fr) * 1991-08-14 1993-02-17 Linde Aktiengesellschaft Procédé et dispositif de rectification d'air
EP0540900A1 (fr) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Système de rectification cryogénique pour la production d'oxygène ultra-pure
FR2777641A1 (fr) * 1998-04-21 1999-10-22 Air Liquide Procede et installation de distillation d'air avec production d'argon
EP0952415A1 (fr) * 1998-04-21 1999-10-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de distillation d'air avec production variable d'argon
FR2787562A1 (fr) * 1998-12-22 2000-06-23 Air Liquide Procede et installation de distillation d'air avec production d'argon
EP0605262B1 (fr) * 1992-12-30 2000-06-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de production d'oxygène gazeux sous pression

Families Citing this family (19)

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US5129932A (en) * 1990-06-12 1992-07-14 Air Products And Chemicals, Inc. Cryogenic process for the separation of air to produce moderate pressure nitrogen
US5161380A (en) * 1991-08-12 1992-11-10 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification system for enhanced argon production
US5207066A (en) * 1991-10-22 1993-05-04 Bova Vitaly I Method of air separation
US5255522A (en) * 1992-02-13 1993-10-26 Air Products And Chemicals, Inc. Vaporization of liquid oxygen for increased argon recovery
US5245831A (en) * 1992-02-13 1993-09-21 Air Products And Chemicals, Inc. Single heat pump cycle for increased argon recovery
US5228296A (en) * 1992-02-27 1993-07-20 Praxair Technology, Inc. Cryogenic rectification system with argon heat pump
DE69301555T2 (de) * 1992-07-20 1996-08-01 Air Prod & Chem Hochdruckverflüssiger
US5275003A (en) * 1992-07-20 1994-01-04 Air Products And Chemicals, Inc. Hybrid air and nitrogen recycle liquefier
US5305611A (en) * 1992-10-23 1994-04-26 Praxair Technology, Inc. Cryogenic rectification system with thermally integrated argon column
US5311744A (en) * 1992-12-16 1994-05-17 The Boc Group, Inc. Cryogenic air separation process and apparatus
US6082136A (en) * 1993-11-12 2000-07-04 Daido Hoxan Inc. Oxygen gas manufacturing equipment
US5469710A (en) * 1994-10-26 1995-11-28 Praxair Technology, Inc. Cryogenic rectification system with enhanced argon recovery
US6318120B1 (en) * 2000-08-11 2001-11-20 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic distillation system for air separation
EP1300640A1 (fr) * 2001-10-04 2003-04-09 Linde Aktiengesellschaft Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air
US7549301B2 (en) 2006-06-09 2009-06-23 Praxair Technology, Inc. Air separation method
CN100445671C (zh) * 2007-02-12 2008-12-24 庞启东 利用尾气余热的氨水吸收式制冷装置
US8448463B2 (en) * 2009-03-26 2013-05-28 Praxair Technology, Inc. Cryogenic rectification method
FR2953915B1 (fr) * 2009-12-11 2011-12-02 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
CN104406364B (zh) * 2014-11-06 2016-10-05 杭州杭氧股份有限公司 一种双塔耦合的氩气回收纯化设备及氩气回收纯化方法

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Publication number Priority date Publication date Assignee Title
WO1987005098A1 (fr) * 1986-02-20 1987-08-27 Erickson Donald C Production d'oxygene et d'argon par distillation a contre pression
EP0341512B1 (fr) * 1988-04-29 1992-12-02 Air Products And Chemicals, Inc. Système de régulation pour maximiser la récupération de l'argon des unités cryogéniques de séparation d'air

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US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US3079759A (en) * 1961-03-22 1963-03-05 Air Prod & Chem Separation of gaseous mixtures
FR2041701B1 (fr) * 1969-05-05 1974-02-01 Air Liquide
DE1922956B1 (de) * 1969-05-06 1970-11-26 Hoechst Ag Verfahren zur Erzeugung von argonfreiem Sauerstoff durch Rektifikation von Luft
IT1034545B (it) * 1975-03-26 1979-10-10 Siad Processo ed impianto per l otte nimento dell argon a partire da un processo di frazionamento dell aria
DE3436897A1 (de) * 1984-10-08 1986-04-10 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zum betreiben einer luftzerlegungsanlage
DE3770772D1 (de) * 1986-11-24 1991-07-18 Boc Group Plc Luftverfluessigung.

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1987005098A1 (fr) * 1986-02-20 1987-08-27 Erickson Donald C Production d'oxygene et d'argon par distillation a contre pression
EP0341512B1 (fr) * 1988-04-29 1992-12-02 Air Products And Chemicals, Inc. Système de régulation pour maximiser la récupération de l'argon des unités cryogéniques de séparation d'air

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0527501A1 (fr) * 1991-08-14 1993-02-17 Linde Aktiengesellschaft Procédé et dispositif de rectification d'air
EP0540900A1 (fr) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Système de rectification cryogénique pour la production d'oxygène ultra-pure
EP0605262B1 (fr) * 1992-12-30 2000-06-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de production d'oxygène gazeux sous pression
FR2777641A1 (fr) * 1998-04-21 1999-10-22 Air Liquide Procede et installation de distillation d'air avec production d'argon
EP0952415A1 (fr) * 1998-04-21 1999-10-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de distillation d'air avec production variable d'argon
WO1999054673A1 (fr) * 1998-04-21 1999-10-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et installation de distillation d'air avec production d'argon
US6269659B1 (en) 1998-04-21 2001-08-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for air distillation with production of argon
FR2787562A1 (fr) * 1998-12-22 2000-06-23 Air Liquide Procede et installation de distillation d'air avec production d'argon

Also Published As

Publication number Publication date
US5034043A (en) 1991-07-23
EP0384213A3 (en) 1990-10-24
ZA901345B (en) 1992-06-24
CN1025067C (zh) 1994-06-15
JPH02247485A (ja) 1990-10-03
DE59000514D1 (de) 1993-01-14
EP0384213B1 (fr) 1992-12-02
CN1045172A (zh) 1990-09-05

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