EP0768503A2 - Procédé de séparation d'air à triple colonne - Google Patents

Procédé de séparation d'air à triple colonne Download PDF

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Publication number
EP0768503A2
EP0768503A2 EP96116124A EP96116124A EP0768503A2 EP 0768503 A2 EP0768503 A2 EP 0768503A2 EP 96116124 A EP96116124 A EP 96116124A EP 96116124 A EP96116124 A EP 96116124A EP 0768503 A2 EP0768503 A2 EP 0768503A2
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EP
European Patent Office
Prior art keywords
pressure column
pressure
column
low
medium
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
EP96116124A
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German (de)
English (en)
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EP0768503B1 (fr
EP0768503A3 (fr
Inventor
Jürgen Dipl.-Phys. Voit
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
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Linde GmbH
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Filing date
Publication date
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Publication of EP0768503A3 publication Critical patent/EP0768503A3/fr
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Publication of EP0768503B1 publication Critical patent/EP0768503B1/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
    • F25J3/04248—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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate 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
    • F25J3/04763—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
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
    • 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
    • Y10S62/90—Triple column
    • 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
    • Y10S62/939—Partial feed stream expansion, air

Definitions

  • the invention relates to a method for the low-temperature separation of air in a triple column system, which consists of a high-pressure column, a medium-pressure column and a low-pressure column, with the steps (a) to (i) set out in claim 1.
  • a triple column system has at least three columns for nitrogen-oxygen separation.
  • the term includes systems and processes which have further columns for nitrogen-oxygen separation and / or for the production of other air components such as noble gases, for example a crude argon column.
  • a triple column method of the type mentioned above is known from DE-A-2903089. All of the feed air is compressed to a first pressure that is above the medium pressure column pressure, and some of it is fed into the medium pressure column without further pressure-changing measures, another part is further compressed to a second pressure and introduced into the high pressure column. The rest of the compressed feed air is expanded during work and introduced into the low pressure column. However, this process does not work optimally in terms of energy.
  • the invention is therefore based on the object of specifying a method of the type mentioned with particularly high efficiency.
  • This object is achieved in that the first pressure is lower than the operating pressure of the medium pressure column and in that the second part of the feed air is compressed from the first pressure to a third pressure which is at least equal to the operating pressure of the medium pressure column but is lower than the second pressure .
  • the total amount of feed air is therefore only compressed to a relatively low pressure, which is lower than the pressure prevailing in the medium pressure column.
  • the first air part to be introduced into the medium pressure column must be compressed correspondingly higher in a further compressor; that part of the feed air which is fed directly under the low pressure column operating at lower pressure does not need to be brought up to the high pressure of the high pressure column.
  • the cooling requirement of the system is relatively low, for example because a small part of the products is liquid is obtained or it is a pure gas system, there is a particularly low energy consumption.
  • the third part of the feed air is recompressed upstream of the work relaxation to increase the pressure difference during work relaxation.
  • the pressure upon entering work relaxation is preferably between the first pressure and the pressure of the medium pressure column.
  • the energy obtained in the work-relieving relaxation of the third air part or part thereof should be used for the compression of the third air part.
  • the post-compressor is preferably driven exclusively by this internally generated mechanical energy, so that it does not consume any energy introduced from outside.
  • the post-compressor and expansion machine are mechanically coupled, for example, via a common shaft.
  • the high-pressure column can be operated under a relatively low pressure, which is preferably 4.8 bar or less. This results in a particularly low effort when compressing the feed air.
  • the low pressure column is preferably operated under the lowest possible pressure. This is determined by the fact that the top product of the low-pressure column can be removed from the process under essentially atmospheric pressure, if appropriate after passing through one or more heat exchangers; if this overhead product is used as regeneration gas in a cleaning device (e.g. a molecular sieve system), the pressure of the low pressure column must also enable it to operate.
  • a cleaning device e.g. a molecular sieve system
  • part of the first oxygen-enriched bottom fraction is introduced from the high-pressure column into the medium-pressure column. This means that part of the bottom product from the high-pressure column is further broken down, and a larger amount of nitrogen-enriched fraction is obtained at the top of the medium-pressure column, which is available as reflux liquid in the low-pressure column. This further improves rectification in the low pressure column.
  • the bottom fraction from the high-pressure column is preferably introduced into the medium-pressure column at an intermediate point, that is to say at a point which has at least one practical or theoretical floor above the bottom of the medium pressure column and in particular at least one practical or theoretical floor above the point where the second air part is fed into the medium pressure column.
  • the invention also relates to a device for the low-temperature separation of air according to claims 8 to 11.
  • pure nitrogen can also be produced if a conventional pure nitrogen section is additionally arranged at the top of the low-pressure column.
  • Argon extraction is also possible if the low pressure column is followed by argon rectification in a known manner (see for example EP-B-377117).
  • other noble gases can be generated in a known manner.
  • Feed air 1 is compressed in a main air compressor 2 to a first pressure.
  • the compressed feed air 3 is divided into a first partial flow 101, a second partial flow 201 and a third partial flow 301.
  • the first partial flow is brought to a second pressure and the second partial flow is brought to a third pressure lying between the first and the second pressure.
  • the first partial flow and the second partial flow are first compressed together (4) in the compressor 5 to the third pressure and then the first partial flow 101 alone is further compressed in the compressor 102 to the second pressure.
  • the first and the second partial stream can also be compressed independently of one another.
  • the third partial flow which is fed to the expansion machine 305 or the post-compressor 302, can be branched off downstream of one of the compressors 5 or 102.
  • the resulting higher inlet pressure when relaxing allows the cooling capacity to be increased and / or the amount of air blown directly into the low-pressure column to be reduced.
  • the first partial flow 103, which is under the second pressure, and the second partial flow 201, which is under the third pressure, are cooled in a main heat exchanger 6 against product flows and fed into the high-pressure column 7 and into the medium-pressure column 8 (104 and 202, respectively).
  • the high pressure column 7 is operated under a pressure of 4.5 to 5.5 bar, preferably 4.6 to 4.8 bar
  • the medium pressure column 8 is under 2.5 to 3.5 bar, preferably 2.8 to 3.0 bar.
  • the first pressure (in line 3 behind the main air compressor 2) is significantly lower than the high pressure column pressure; the difference is at least 2.5 bar, preferably 3.0 to 3.2 bar.
  • the second pressure is slightly above the high pressure column pressure (for example about 0.1 bar above the pressure at the feed point into the high pressure column) in order to compensate for the pressure drop in the main heat exchanger 6 and in the lines 103 and 104.
  • the third pressure (downstream of the compressor 5) is slightly above the pressure of the medium pressure column in order to ensure the introduction of the second partial flow 201, 202 into the medium pressure column 8.
  • the third partial flow 301 is optionally post-compressed in a post-compressor 302 to a fourth pressure, which can be between the first pressure and the operating pressure of the medium-pressure column and is, for example, 1.5 to 2.5 bar higher than the first pressure.
  • the fourth pressure is correspondingly higher, that is to say, for example, higher than the pressure of the medium pressure column or even higher than the pressure of the high pressure column; in this case it can be up to to 8 bar or more.
  • Via line 303 it goes to the main heat exchanger 6 and from its cold end further (304) to the relaxation machine 305.
  • the work-relieved air 306 is introduced into the low-pressure column 9 at medium height.
  • each compressor 2, 5, 102, 302 The air is cooled behind each compressor 2, 5, 102, 302 in indirect heat exchange with cooling water, as indicated by the aftercoolers shown in the drawing.
  • intermediate cooling is preferably carried out between two stages.
  • a first nitrogen-enriched top fraction is obtained as the top gas and a first oxygen-enriched fraction as the bottom liquid.
  • Top gas 10 is condensed in a first condenser-evaporator 11 and in part 12 in the high pressure column and in another part 13 - if necessary after subcooling in countercurrent 14 - throttled via line 15 into the low-pressure column 9 (16), the operating pressure of which is 1.1 to 1.5 bar, preferably 1.2 to 1.4 bar.
  • a part of the condensed nitrogen-enriched fraction 13 from the high pressure column can be led via the optional line 17 to the top of the medium pressure column 8.
  • the bottom liquid of the high-pressure column is also released via line 18 into the low-pressure column 9 after optional subcooling (14) (19, 20).
  • the feed point is above that of the air 306 which has been relieved of work.
  • a portion 37 (10 to 30%, preferably 15 to 20%) of the high-pressure column bottom liquid 18 is led into the medium-pressure column.
  • the feed point is at least one practical or theoretical floor, preferably two to five theoretical floors above the feed of the second air part 202.
  • a second nitrogen-enriched top fraction and a second oxygen-enriched bottom liquid are obtained in the medium-pressure column 8.
  • the top gas 21 is condensed in a second condenser-evaporator 22 and throttled to a first part 23 in the medium pressure column and to a second part 24 - possibly after subcooling in countercurrent 14 - in the low pressure column 9 (25).
  • the bottom liquid of the medium-pressure column is expanded via line 26, likewise after optional supercooling (14), into the evaporation space of the second condenser-evaporator 22 (27).
  • the vaporized stream 28 is introduced into the low pressure column 9 (29).
  • the feed point for example, at the same level as that of the sump liquid from the high pressure column or slightly above.
  • Steam 31 for the rectification in the low-pressure column 9 is generated by evaporating bottom liquid 30 in the first condenser-evaporator 11.
  • the condenser-evaporator 11 can be arranged differently from the illustration in the bottom of the low-pressure column 9.
  • nitrogen 32 leaves the low-pressure column 9 is warmed to approximately ambient temperature in the heat exchangers 14 and 6, and is withdrawn at 33.
  • Gaseous product oxygen 35 is removed via line 34 and also heated in the main heat exchanger 6. If necessary, the oxygen product or a part thereof can be withdrawn in liquid form (line 36).
  • the liquid oxygen removed can be pressurized and evaporated (internal compression).
  • the cleaning of the feed air is not shown in the drawing. It can be carried out by any of the known methods, for example in a switchable one Heat exchanger (Revex) or in one or more molecular sieve systems. In the latter case, it is possible to subject the entire feed air (line 3) to cleaning together, to treat the three partial streams 103, 201, 303 in separate systems, or also to jointly treat the first and second partial streams by a compressor immediately downstream of the aftercooler of the compressor 5 to send arranged molecular sieve. In the event that, contrary to the illustration in the drawing, the third partial flow behind one of the compressors 5 or 102 is removed and fed to the post-compressor 302, all three partial flows or at least the first and the third partial flow can be cleaned together.
  • Revex Heat exchanger
  • molecular sieve systems molecular sieve
  • the mass transfer elements in the high-pressure column and in the medium-pressure column are formed by still bottoms, those in the low-pressure column by orderly packing.
  • conventional still bottoms, packing (unordered packing) and / or ordered packing can be used in each of the columns in the invention. Combinations of different types of elements in one column are also possible. Because of the low pressure drop, ordered packings in all columns, especially in the low pressure column, are preferred. These further increase the energy-saving effect of the invention.
  • Table 1 for the production of pure oxygen (99.5%) and Table 2 for the production of medium purity oxygen (95.0%).

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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)
EP96116124A 1995-10-11 1996-10-09 Procédé de séparation d'air à triple colonne Expired - Lifetime EP0768503B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19537913A DE19537913A1 (de) 1995-10-11 1995-10-11 Dreifachsäulenverfahren zur Tieftemperaturzerlegung von Luft
DE19537913 1995-10-11

Publications (3)

Publication Number Publication Date
EP0768503A2 true EP0768503A2 (fr) 1997-04-16
EP0768503A3 EP0768503A3 (fr) 1998-02-04
EP0768503B1 EP0768503B1 (fr) 2001-07-25

Family

ID=7774605

Family Applications (1)

Application Number Title Priority Date Filing Date
EP96116124A Expired - Lifetime EP0768503B1 (fr) 1995-10-11 1996-10-09 Procédé de séparation d'air à triple colonne

Country Status (3)

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US (1) US5730004A (fr)
EP (1) EP0768503B1 (fr)
DE (2) DE19537913A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0838647A3 (fr) * 1996-10-25 1998-10-21 Air Products And Chemicals, Inc. Production cryogénique à trois colonnes d'oxygène impur et d'azote pur
FR2774753A1 (fr) * 1998-02-06 1999-08-13 Air Liquide Installation de distillation d'air comprenant plusieurs unites de distillation cryogenique de meme nature
GB2334085B (en) * 1998-02-06 2001-12-12 Air Liquide Air distillation plant
DE19933558B4 (de) * 1999-07-16 2007-09-13 Linde Ag Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6205815B1 (en) 1997-04-11 2001-03-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Plant for separation of a gas mixture by distillation
DE10103968A1 (de) * 2001-01-30 2002-08-01 Linde Ag Drei-Säulen-System zur Tieftemperaturzerlegung von Luft
DE10113790A1 (de) * 2001-03-21 2002-09-26 Linde Ag Drei-Säulen-System zur Tieftemperatur-Luftzerlegung
US6397631B1 (en) * 2001-06-12 2002-06-04 Air Products And Chemicals, Inc. Air separation process
EP2235460B1 (fr) * 2008-01-28 2018-06-20 Linde Aktiengesellschaft Procédé et installation pour la séparation cryogénique d'air
DE102009023900A1 (de) 2009-06-04 2010-12-09 Linde Aktiengesellschaft Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
FR2946735B1 (fr) * 2009-06-12 2012-07-13 Air Liquide Appareil et procede de separation d'air par distillation cryogenique.
FR2953915B1 (fr) * 2009-12-11 2011-12-02 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US8978413B2 (en) * 2010-06-09 2015-03-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Rare gases recovery process for triple column oxygen plant

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2854508C2 (de) * 1978-12-16 1981-12-03 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zur Tieftemperaturzerlegung eines Gasgemisches
DE2903089A1 (de) * 1979-01-26 1980-07-31 Linde Ag Verfahren zur gewinnung von sauerstoff aus luft
DE3817244A1 (de) * 1988-05-20 1989-11-23 Linde Ag Verfahren zur tieftemperaturzerlegung von luft
DE3840506A1 (de) * 1988-12-01 1990-06-07 Linde Ag Verfahren und vorrichtung zur luftzerlegung
US5069699A (en) * 1990-09-20 1991-12-03 Air Products And Chemicals, Inc. Triple distillation column nitrogen generator with plural reboiler/condensers
US5233838A (en) * 1992-06-01 1993-08-10 Praxair Technology, Inc. Auxiliary column cryogenic rectification system
GB9213776D0 (en) * 1992-06-29 1992-08-12 Boc Group Plc Air separation
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
US5341646A (en) * 1993-07-15 1994-08-30 Air Products And Chemicals, Inc. Triple column distillation system for oxygen and pressurized nitrogen production
GB9325648D0 (en) * 1993-12-15 1994-02-16 Boc Group Plc Air separation
US5386692A (en) * 1994-02-08 1995-02-07 Praxair Technology, Inc. Cryogenic rectification system with hybrid product boiler
GB9414939D0 (en) * 1994-07-25 1994-09-14 Boc Group Plc Air separation
GB9414938D0 (en) * 1994-07-25 1994-09-14 Boc Group Plc Air separation

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0838647A3 (fr) * 1996-10-25 1998-10-21 Air Products And Chemicals, Inc. Production cryogénique à trois colonnes d'oxygène impur et d'azote pur
FR2774753A1 (fr) * 1998-02-06 1999-08-13 Air Liquide Installation de distillation d'air comprenant plusieurs unites de distillation cryogenique de meme nature
GB2334085B (en) * 1998-02-06 2001-12-12 Air Liquide Air distillation plant
DE19904527B4 (de) * 1998-02-06 2007-07-05 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Luftdestillationsanlage mit mehreren kryogenen Destillationseinheiten des gleichen Typs
DE19904526B4 (de) * 1998-02-06 2008-06-26 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Luftdestillationsanlage und zugehörige Kältebox
DE19964549B4 (de) * 1998-02-06 2010-07-15 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Luftdestillationsanlage und zugehörige Kältebox
DE19933558B4 (de) * 1999-07-16 2007-09-13 Linde Ag Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
DE19933558C5 (de) * 1999-07-16 2010-04-15 Linde Ag Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft

Also Published As

Publication number Publication date
DE59607348D1 (de) 2001-08-30
EP0768503B1 (fr) 2001-07-25
EP0768503A3 (fr) 1998-02-04
DE19537913A1 (de) 1997-04-17
US5730004A (en) 1998-03-24

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