EP1189003B1 - Procédé et installation de séparation d'air par distillation cryogénique - Google Patents

Procédé et installation de séparation d'air par distillation cryogénique Download PDF

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Publication number
EP1189003B1
EP1189003B1 EP01402310A EP01402310A EP1189003B1 EP 1189003 B1 EP1189003 B1 EP 1189003B1 EP 01402310 A EP01402310 A EP 01402310A EP 01402310 A EP01402310 A EP 01402310A EP 1189003 B1 EP1189003 B1 EP 1189003B1
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EP
European Patent Office
Prior art keywords
pressure column
low
column
pressure
oxygen
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.)
Expired - Lifetime
Application number
EP01402310A
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German (de)
English (en)
French (fr)
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EP1189003A1 (fr
Inventor
Benoit Davidian
Francois De Bussy
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.)
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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Publication of EP1189003A1 publication Critical patent/EP1189003A1/fr
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Publication of EP1189003B1 publication Critical patent/EP1189003B1/fr
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J3/04248—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
    • F25J3/04309—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 nitrogen
    • 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
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air

Definitions

  • the present invention relates to a method and an installation of air separation by cryogenic distillation according to the preamble of claims 1 and 9, respectively.
  • Such a process and such installation are known from US-A-5,657,644.
  • An object of the invention is to reduce the energy consumption of the process separation from the prior art methods.
  • Another object of the invention is to produce oxygen with a purity of minus 95 mol%, or even at least 98 mol%. with improved performance.
  • Figure 1 shows a conventional method with a low pressure column 103 operating at 1.3 bara to make oxygen at 99.5 mol%. with a 92% yield.
  • a flow rate of 1000 Nm 3 / h of air 1 at approximately 5 bara is divided in two to form a first flow 17 and a second flow 3 which is supercharged in a booster 5 at a higher pressure of the order of 75 bara. .
  • Both flow rates 3.17 cool through crossing a heat exchanger 100.
  • flow 17 is sent to the tank of the high pressure column 101 and the liquefied flow 3 in the exchanger 100 is expanded in a turbine 6 producing a flow at least partially liquid at its outlet, the fluid or mixture of fluids leaving the turbine 6 being sent at least in part to the high pressure column 101.
  • a flow of rich liquid 10 from the high pressure column 101 cools in the subcooler 83 before being relaxed and sent to an intermediate level of the low pressure column 103.
  • a liquid air flow 12 is withdrawn from the high pressure column 101, cooled in the subcooler 83, expanded and sent to the low pressure column 103.
  • a flow of residual nitrogen 72 is withdrawn at the top of the low pressure column 103, sent to the subcooler 83 and then to the exchanger 100 where it heats up.
  • a flow rate of 193 Nm 3 / h of oxygen at 99.5 mol%. is withdrawn in liquid form from the low pressure column 103, pumped into the pump 19 to 40 bara and vaporizes in the exchanger 100 to form a gas flow under pressure.
  • a flow rate of 200 Nm 3 / h of nitrogen gas 33 is withdrawn from the top of the high pressure column 101 and is partially heated in the exchanger 100. At an intermediate temperature, part of the gas is expanded in a turbine 35 before to be mixed with the waste gas 72.
  • a flow rate of 1000 Nm 3 / h of air 1 to about 14.3 bara is divided in two to form a first flow 17 and a second flow 3 which is supercharged in a booster 5 at a higher pressure of the order of 75 bara.
  • Both flow rates 3.17 cool through crossing a heat exchanger 100.
  • flow 17 is sent to the tank of the high pressure column 101 and the liquid flow 3 is expanded in a turbine 6 producing a flow at least rectally liquid at its outlet, the fluid or mixture of fluids leaving the turbine 6 being sent at least part of the high pressure column 101.
  • a flow of rich liquid 10 from the high pressure column 101 cools in the subrefroder 83 before being relaxed and sent to an intermediate level of the low pressure column 103.
  • a liquid air flow 12 is withdrawn from the high pressure column 101, cooled in the subcooler 83, expanded and sent to the low pressure column 103.
  • a flow of residual nitrogen 72 is withdrawn at the top of the low pressure column 103, sent to the subcooler 83 and then to the exchanger 100 where it heats up.
  • a flow 31 of 164 Nm 3 / h of oxygen at 99.5 mol%. is withdrawn in liquid form from the low pressure column, pumped into the pump 19 to 40 bara and vaporizes in the exchanger 100 to form a gas flow under pressure.
  • a separation installation of air by cryogenic distillation comprising a high pressure column, a column at intermediate pressure having a bottom reboiler and a low pressure column, the high pressure column and the low pressure column being thermally connected between them, means for sending a mixture of at least oxygen, nitrogen and argon at least to the high pressure column, means for sending a flow enriched with oxygen from the high pressure column to the intermediate pressure column, means for sending an oxygen-enriched fluid and / or a nitrogen-enriched fluid from the intermediate pressure column to the low pressure column, means for send a fluid from the low pressure column to the bottom reboiler of the column to intermediate pressure, means for withdrawing a nitrogen-enriched fluid and a fluid enriched with oxygen in the low pressure column, characterized in that it does not include means for enriching argon with a fluid containing between 3 and 20 mol% argon other than high pressure, low pressure and pressure columns intermediate.
  • the fluid sent to the reboiler is withdrawn from the column low pressure at a level lower than the level of the introduction of a fluid enriched in oxygen from the intermediate pressure column.
  • the intermediate pressure column has a head condenser.
  • the fluids known as 'enriched in oxygen' or 'enriched in nitrogen' are enriched in these components compared to air.
  • the apparatus operates with a low column pressure at 1.3 bara and in the case of Figure 4, the apparatus operates with a low pressure column at 4.8 bara.
  • the installation of Figure 3 includes a high pressure column 101 operating at 5 bara, an intermediate pressure column 102 operating at 2.7 bara and a low pressure column 103 operating at 1.3 bara.
  • Part of the nitrogen gas head of the high pressure column is used to heat the bottom reboiler of the column pressure but other means of heating can be envisaged, such as double reboiler systems, one heated by air.
  • a flow rate of 1000 Nm 3 / h of air 1 at approximately 5 bara is divided in two to form a first flow 17 and a second flow 3 which is supercharged in a booster 5 at a higher pressure of the order of 75 bara. .
  • Both flow rates 3.17 cool through crossing a heat exchanger 100.
  • flow 17 is sent to the tank of the high pressure column 101 without being relaxed or compressed and the liquid flow 3 is expanded in a turbine 6 producing a flow rate at less partially liquid at its outlet, the fluid or mixture of fluids leaving the turbine 6 being sent at least in part to the high pressure column 101.
  • a flow of rich liquid 10 from the high pressure column 101 cools in the subcooler 83 before being relaxed and sent to an intermediate level of the intermediate pressure column 102 between two sections, for example of structured packings of corrugated-cross type.
  • the liquid can be sent to another level of the column and the column can also receive a gaseous air flow or liquid.
  • This liquid is separated into a second oxygen-enriched liquid 20 and a nitrogen-enriched liquid 25.
  • the liquid 25 cools in the subcooler 83, before to be relaxed and sent to the top of the low pressure column 103, after being mixed with a poor liquid flow 15 from the top of the high pressure column 101 which was also cooled in the subcooler 83 and relaxed in a valve.
  • the bottom liquid of the intermediate pressure column is divided into two. Part is relaxed and sent to the low pressure column directly while the rest is expanded in a valve, sent to the head condenser 29 of the intermediate pressure column where it vaporizes at least partially before to be sent to the low pressure column 103.
  • a liquid air flow 12 is withdrawn from the high pressure column, cooled in the subcooler 83, expanded and sent to the low pressure column 103.
  • the reboiler 24 of the intermediate pressure column 102 is heated by means of an argon-enriched gas flow 233 containing about 5 to 15% mol., preferably between 8 and 10 mol%. argon from the lower column pressure 103. This flow condenses at least partially in the reboiler 24 before being returned to the low pressure column 103
  • a flow of residual nitrogen 72 is withdrawn at the top of the low pressure column 103, sent to the subcooler 83 and then to the exchanger 100 where it heats up.
  • a flow rate of 203 Nm 3 / h of oxygen at 99.5 mol%. is withdrawn in liquid form from the low pressure column 103, pumped into the pump 19 to 40 bara and vaporizes in the exchanger 100 to form a gas flow under pressure.
  • a flow rate of 200 Nm 3 / h of nitrogen gas is withdrawn at the top of the high pressure column 101 and is partially heated in the exchanger 100. At an intermediate temperature, part of the gas is expanded in a turbine 35 before mixed with the waste gas 72. The rest of the nitrogen continues its heating and is a product of the apparatus.
  • FIG. 4 The installation of Figure 4 includes a high pressure column 101 operating at 14.3 bara, an intermediate pressure column 102 operating at 8.5 bara and a low pressure column 103 operating at 4.8 bara. All the nitrogen gas in the head of the high pressure column is used to heat the bottom column reboiler pressure but other means of heating can be envisaged, such as double reboiler systems, one heated by air.
  • a flow rate of 1000 Nm 3 / h of air 1 to about 14.3 bara is divided in two to form a first flow 17 and a second flow 3 which is supercharged in a booster 5 at a higher pressure of the order of 75 bara.
  • Both flow rates 3.17 cool through crossing a heat exchanger 100.
  • flow 17 is sent to the tank of the high pressure column 101 and the liquid flow 3 is expanded in a turbine producing a flow at least partially liquid at its outlet, the fluid or mixture of fluids leaving the turbine being sent at least part of the high pressure column 101.
  • a flow of rich liquid 10 from the high pressure column 101 cools in the subcooler 83 before being relaxed and sent to an intermediate level of the intermediate pressure column 102 between two sections, for example of structured packings of corrugated-cross type.
  • the liquid can be sent to another level of the column and the column can also receive a gaseous air flow or liquid.
  • This liquid is separated into a second oxygen-enriched liquid 20 and a nitrogen-enriched liquid 25.
  • the liquid 25 cools in the subcooler 83, before to be relaxed and sent to the top of the low pressure column 103, after being mixed with a poor liquid flow 15 from the top of the high pressure column 101 which was also cooled in the subcooler 83 and relaxed in a valve.
  • the bottom liquid of the intermediate pressure column is divided into two. Part is relaxed and sent to the low pressure column directly while the rest is relaxed in a valve, sent to the head condenser 22 of the intermediate pressure column where it vaporizes at least partially before to be sent to the low pressure column 103.
  • a liquid air flow 12 is withdrawn from the high pressure column, cooled in the subcooler 83, expanded and sent to the low pressure column.
  • the reboiler 24 of the intermediate pressure column 102 is heated by means of an argon-enriched gas flow 233 containing about 5 to 15% mol., preferably 8 to 10 mol%. argon from the low pressure column 103. This flow is condensed at least partially in the reboiler 24 before being returned to the low pressure column 103.
  • a flow of residual nitrogen 72 is withdrawn at the top of the low pressure column 103, sent to the subcooler 83 and then to the exchanger 100 where it heats up.
  • a flow 31 of 177 Nm 3 / h of oxygen at 99.5 mol%. is withdrawn in liquid form from the low pressure column, pumped into the pump 19 to 40 bara and vaporizes in the exchanger 100 to form a gas flow under pressure.
  • the apparatus may receive all or a portion of its supply air from a compressor of a gas turbine, the residual nitrogen of the apparatus being returned to the gas turbine.

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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)
EP01402310A 2000-09-19 2001-09-06 Procédé et installation de séparation d'air par distillation cryogénique Expired - Lifetime EP1189003B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0011932A FR2814229B1 (fr) 2000-09-19 2000-09-19 Procede et installation de separation d'air par distillation cryogenique
FR0011932 2000-09-19

Publications (2)

Publication Number Publication Date
EP1189003A1 EP1189003A1 (fr) 2002-03-20
EP1189003B1 true EP1189003B1 (fr) 2005-01-26

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EP01402310A Expired - Lifetime EP1189003B1 (fr) 2000-09-19 2001-09-06 Procédé et installation de séparation d'air par distillation cryogénique

Country Status (7)

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US (1) US6536232B2 (xx)
EP (1) EP1189003B1 (xx)
AT (1) ATE288064T1 (xx)
CA (1) CA2357302A1 (xx)
DE (1) DE60108579T2 (xx)
FR (1) FR2814229B1 (xx)
ZA (1) ZA200107210B (xx)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ES2278703T5 (es) * 2001-12-04 2010-03-17 Air Products And Chemicals, Inc. Proceso y aparato para la separacion criogenica de aire.
FR2875588B1 (fr) * 2004-09-21 2007-04-27 Air Liquide Procede de separation d'air par distillation cryogenique
DE102004047961A1 (de) * 2004-10-01 2006-05-18 Siemens Ag Vorrichtung und Verfahren zum Ansteuern eines Piezoaktors
EP2597409B1 (en) * 2011-11-24 2015-01-14 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and apparatus for the separation of air by cryogenic distillation
EP2634517B1 (en) * 2012-02-29 2018-04-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and apparatus for the separation of air by cryogenic distillation
FR3017698B1 (fr) * 2014-02-14 2019-03-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Colonne de separation d'air par distillation cryogenique, appareil de separation d'air comportant une telle colonne et procede de fabrication d'une telle colonne
EP3620739A1 (de) 2018-09-05 2020-03-11 Linde Aktiengesellschaft Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage
US20240035745A1 (en) 2022-07-28 2024-02-01 Neil M. Prosser System and method for cryogenic air separation using four distillation columns including an intermediate pressure column
US20240035744A1 (en) 2022-07-28 2024-02-01 Neil M. Prosser Air separation unit and method for production of nitrogen and argon using a distillation column system with an intermediate pressure kettle column
US20240035741A1 (en) 2022-07-28 2024-02-01 Neil M. Prosser Air separation unit and method for cryogenic separation of air using a distillation column system including an intermediate pressure kettle column
US11959701B2 (en) 2022-07-28 2024-04-16 Praxair Technology, Inc. Air separation unit and method for production of high purity nitrogen product using a distillation column system with an intermediate pressure kettle column

Family Cites Families (9)

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Publication number Priority date Publication date Assignee Title
US4605427A (en) * 1983-03-31 1986-08-12 Erickson Donald C Cryogenic triple-pressure air separation with LP-to-MP latent-heat-exchange
US5341646A (en) * 1993-07-15 1994-08-30 Air Products And Chemicals, Inc. Triple column distillation system for oxygen and pressurized nitrogen production
GB9412182D0 (en) * 1994-06-17 1994-08-10 Boc Group Plc Air separation
US5682764A (en) * 1996-10-25 1997-11-04 Air Products And Chemicals, Inc. Three column cryogenic cycle for the production of impure oxygen and pure nitrogen
GB9726954D0 (en) * 1997-12-19 1998-02-18 Wickham Michael Air separation
US5881570A (en) * 1998-04-06 1999-03-16 Praxair Technology, Inc. Cryogenic rectification apparatus for producing high purity oxygen or low purity oxygen
US6196024B1 (en) * 1999-05-25 2001-03-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic distillation system for air separation
US6347534B1 (en) * 1999-05-25 2002-02-19 Air Liquide Process And Construction Cryogenic distillation system for air separation
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

Also Published As

Publication number Publication date
CA2357302A1 (fr) 2002-03-19
DE60108579D1 (de) 2005-03-03
EP1189003A1 (fr) 2002-03-20
US20020053219A1 (en) 2002-05-09
US6536232B2 (en) 2003-03-25
DE60108579T2 (de) 2005-12-22
ZA200107210B (en) 2002-03-04
FR2814229A1 (fr) 2002-03-22
FR2814229B1 (fr) 2002-10-25
ATE288064T1 (de) 2005-02-15

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