EP1189003A1 - Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation - Google Patents

Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation Download PDF

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Publication number
EP1189003A1
EP1189003A1 EP01402310A EP01402310A EP1189003A1 EP 1189003 A1 EP1189003 A1 EP 1189003A1 EP 01402310 A EP01402310 A EP 01402310A EP 01402310 A EP01402310 A EP 01402310A EP 1189003 A1 EP1189003 A1 EP 1189003A1
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EP
European Patent Office
Prior art keywords
pressure column
column
enriched
flow
oxygen
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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
EP01402310A
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English (en)
French (fr)
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EP1189003B1 (de
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 pour lEtude et lExploitation des Procedes Georges Claude
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude, LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP1189003A1 publication Critical patent/EP1189003A1/de
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Publication of EP1189003B1 publication Critical patent/EP1189003B1/de
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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 for air separation by cryogenic distillation.
  • it relates to a process using three separation columns operating at high pressure, low pressure and an intermediate pressure between high and low pressures.
  • An object of the invention is to reduce the energy consumption of the process separation with respect to the methods of the prior art.
  • Another object of the invention is to produce oxygen with a purity of at least minus 95% mol., or even at least 98% mol. with improved performance.
  • Figure 1 shows a typical process with a low pressure column 103 operating at 1.3 bara making oxygen at 99.5% mol. with a 92% yield.
  • a flow of 1000 Nm 3 / h of air 1 at around 5 bara is divided into two to form a first flow 17 and a second flow 3 which is boosted in a booster 5 at a higher pressure of the order of 75 bara .
  • the flow 17 is sent to the tank of the high pressure column 101 and flow 3 liquefied 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 expanded 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 residual nitrogen flow 72 is drawn off at the head 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 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 at 40 bara and vaporized 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 head 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 d 'be mixed with waste gas 72.
  • a flow of 1000 Nm 3 / h of air 1 at around 14.3 bara is divided into two to form a first flow 17 and a second flow 3 which is boosted in a booster 5 at a higher pressure of the order of 75 bara.
  • the two flows 3.17 cool by passing through an exchanger 100.
  • the 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 an at least partially liquid flow 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 sub-cooler 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 residual nitrogen flow 72 is drawn off at the head 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 at 40 bara and vaporized in the exchanger 100 to form a gas flow under pressure.
  • the inventors of the present application have discovered that even without using an argon separation column, the purification of oxygen in the bottom of the column low pressure remains satisfactory for the production of high purity oxygen.
  • a separation installation air by cryogenic distillation comprising a high pressure column, a column at intermediate pressure having a tank reboiler and a low pressure column, the high pressure column and the low pressure column being thermally connected between them, means for sending at least a mixture of oxygen, nitrogen and argon at least to the high pressure column, means for sending a flow enriched in 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 column reboiler of the column to intermediate pressure, means for withdrawing a nitrogen-enriched fluid and a fluid enriched in oxygen from the low pressure column, characterized in that it does not includes no 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 introduction of a fluid enriched in oxygen from the intermediate pressure column.
  • the intermediate pressure column has an overhead condenser.
  • Fluids called 'enriched in oxygen' or 'enriched in nitrogen' are enriched in these components compared to air.
  • the device operates with a low column pressure at 1.3 bara and in the case of Figure 4, the device operates with a low pressure column at 4.8 bara.
  • FIG. 3 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 overhead nitrogen gas 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 of which is heated by air.
  • a flow of 1000 Nm 3 / h of air 1 at around 5 bara is divided into two to form a first flow 17 and a second flow 3 which is boosted in a booster 5 at a higher pressure of the order of 75 bara .
  • the two flows 3.17 cool by passing through an exchanger 100.
  • the flow 17 is sent to the tank of the high pressure column 101 without having been expanded or compressed and the liquid flow 3 is expanded in a turbine 6 producing a flow 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 expanded and sent to an intermediate level of the intermediate pressure column 102 between two sections, for example of structured fillings of wavy-cross type. Liquid can be sent to another column level and the column can also receive a flow of gaseous air or liquid.
  • This liquid is separated into a second oxygen-enriched liquid 20 and a liquid enriched in nitrogen 25.
  • the liquid 25 cools in the subcooler 83, before to be relaxed and sent to the head of the low pressure column 103, after being mixed with a lean liquid flow 15 from the head of the high pressure column 101 which has also been cooled in the subcooler 83 and expanded in a valve.
  • the tank liquid 20 of the intermediate pressure column is divided into of them. A part is relaxed and sent to the low pressure column directly while the rest is expanded 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 103.
  • the tank reboiler 24 of the intermediate pressure column 102 is heated by means of a gas flow enriched in argon 233 containing approximately 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 residual nitrogen flow 72 is drawn off at the head 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 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 at 40 bara and vaporized in the exchanger 100 to form a gas flow under pressure.
  • a flow 33 of 200 Nm 3 / h of nitrogen gas is drawn off at the head 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 be mixed with the waste gas 72. The rest of the nitrogen continues to heat up and constitutes a product of the apparatus.
  • Liquid products can be drawn from the appliance, but the appliance does not produces no argon-rich fluid.
  • 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 overhead high pressure column is used to heat the bottom column tank reboiler pressure but other means of heating can be envisaged, such as double reboiler systems, one of which is heated by air.
  • a flow of 1000 Nm 3 / h of air 1 at around 14.3 bara is divided into two to form a first flow 17 and a second flow 3 which is boosted in a booster 5 at a higher pressure of the order of 75 bara.
  • the two flows 3.17 cool by passing through an exchanger 100.
  • the flow 17 is sent to the tank of the high pressure column 101 and the liquid flow 3 is expanded in a turbine producing an at least partially liquid flow at its outlet, the fluid or mixture of fluids leaving the turbine 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 expanded and sent to an intermediate level of the intermediate pressure column 102 between two sections, for example of structured fillings of wavy-cross type. Liquid can be sent to another column level and the column can also receive a flow of gaseous air or liquid.
  • This liquid is separated into a second oxygen-enriched liquid 20 and a liquid enriched in nitrogen 25.
  • the liquid 25 cools in the subcooler 83, before to be relaxed and sent to the head of the low pressure column 103, after being mixed with a lean liquid flow 15 from the head of the high pressure column 101 which has also been cooled in the subcooler 83 and expanded in a valve.
  • the tank liquid 20 of the intermediate pressure column is divided into of them. A part is relaxed and sent to the low pressure column directly while the rest is expanded 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 tank reboiler 24 of the intermediate pressure column 102 is heated by means of a gas flow enriched in argon 233 containing approximately 5 to 15% mol., preferably 8 to 10% mol. argon from the low pressure column 103. This flow condenses at least partially in the reboiler 24 before being returned to low pressure column 103.
  • a residual nitrogen flow 72 is drawn off at the head 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 at 40 bara and vaporized in the exchanger 100 to form a gas flow under pressure.
  • the appliance can receive all or part of its supply air from a compressor of a gas turbine, the residual nitrogen from the appliance being returned to the gas turbine.
  • Figure 1 process Figure 3 process (invention) High pressure column pressure 5 bara 5 bara Low pressure column pressure 1.3 bara 1.3 bara Intermediate pressure column pressure 2.7 bara Total treated air flow 1000 Nm 3 / h 1000 Nm 3 / h Oxygen content of the gaseous product 99.5% O2 99.5% O2 Oxygen production, counted pure 193 Nm 3 / h 203 Nm 3 / h High pressure nitrogen gas production 200 Nm 3 / h 200 Nm 3 / h Oxygen extraction efficiency 92% 97% Separation energy Base: 100 95 Figure 2 process Figure 4 process (invention) High pressure column pressure 14.3 bara 14.3 bara Low pressure column pressure 4.8 bara 4.8 bara Intermediate pressure column pressure 8.5 bara Total air flow 1000 Nm 3 / h 1000 Nm 3 / h Oxygen content of the gaseous product 99.

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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 Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation Expired - Lifetime EP1189003B1 (de)

Applications Claiming Priority (2)

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

Publications (2)

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

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EP01402310A Expired - Lifetime EP1189003B1 (de) 2000-09-19 2001-09-06 Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation

Country Status (7)

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

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2634517A1 (de) * 2012-02-29 2013-09-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Vorrichtung zur Trennung von Luft durch kryogenische Destillation
CN106211791A (zh) * 2014-02-14 2016-12-07 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏来分离空气的塔，包括这样的塔的空气分离设备以及用于生产这样的塔的方法
EP3620739A1 (de) * 2018-09-05 2020-03-11 Linde Aktiengesellschaft Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage

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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 (de) * 2011-11-24 2015-01-14 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturdestillation
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
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
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
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

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EP0687876A1 (de) * 1994-06-17 1995-12-20 The BOC Group plc Lufttrennung
EP0924486A2 (de) * 1997-12-19 1999-06-23 The BOC Group plc Lufttrennung

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US5341646A (en) * 1993-07-15 1994-08-30 Air Products And Chemicals, Inc. Triple column distillation system for oxygen and pressurized nitrogen production
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
US5881570A (en) * 1998-04-06 1999-03-16 Praxair Technology, Inc. Cryogenic rectification apparatus for producing high purity oxygen or low purity oxygen
US6347534B1 (en) * 1999-05-25 2002-02-19 Air Liquide Process And Construction Cryogenic distillation system for air separation
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
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

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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
EP0687876A1 (de) * 1994-06-17 1995-12-20 The BOC Group plc Lufttrennung
EP0924486A2 (de) * 1997-12-19 1999-06-23 The BOC Group plc Lufttrennung

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2634517A1 (de) * 2012-02-29 2013-09-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Vorrichtung zur Trennung von Luft durch kryogenische Destillation
US9360250B2 (en) 2012-02-29 2016-06-07 L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude Process and apparatus for the separation of air by cryogenic distillation
CN106211791A (zh) * 2014-02-14 2016-12-07 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏来分离空气的塔，包括这样的塔的空气分离设备以及用于生产这样的塔的方法
CN106211791B (zh) * 2014-02-14 2019-12-31 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏来分离空气的塔，包括这样的塔的空气分离设备以及用于生产这样的塔的方法
EP3620739A1 (de) * 2018-09-05 2020-03-11 Linde Aktiengesellschaft Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage
WO2020048634A1 (de) 2018-09-05 2020-03-12 Linde Aktiengesellschaft Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage

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FR2814229B1 (fr) 2002-10-25
EP1189003B1 (de) 2005-01-26
US6536232B2 (en) 2003-03-25
US20020053219A1 (en) 2002-05-09
CA2357302A1 (fr) 2002-03-19
ZA200107210B (en) 2002-03-04
DE60108579D1 (de) 2005-03-03
FR2814229A1 (fr) 2002-03-22
ATE288064T1 (de) 2005-02-15
DE60108579T2 (de) 2005-12-22

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