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US20060037357A1 - Process and system for obtaining a gaseous pressure product by the cryogenic separation of air - Google Patents

Process and system for obtaining a gaseous pressure product by the cryogenic separation of air Download PDF

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Publication number
US20060037357A1
US20060037357A1 US11/205,035 US20503505A US2006037357A1 US 20060037357 A1 US20060037357 A1 US 20060037357A1 US 20503505 A US20503505 A US 20503505A US 2006037357 A1 US2006037357 A1 US 2006037357A1
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US
United States
Prior art keywords
liquid
product
distillation column
pump
column system
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.)
Abandoned
Application number
US11/205,035
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English (en)
Inventor
Ulrich Ewert
Gerhard Pompl
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
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: EWERT, ULRICH, POMPL, GERHARD
Publication of US20060037357A1 publication Critical patent/US20060037357A1/en
Abandoned legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04818—Start-up of the process
    • 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
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • 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
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the invention relates to a process for obtaining a gaseous pressure product by the cryogenic separation of air.
  • Preferred embodiments of the invention relate to such a process and system wherein, in a normal operation: charge air is condensed, cooled and fed to a distillation column system, a product fraction is withdrawn in a liquid state from the distillation column system and is introduced into a liquid tank, product liquid is removed from the liquid tank via a pump set having one or more parallel-connected individual pumps, is brought in the liquid condition to an increased pressure, is evaporated in an indirect heat exchange with a first heat transfer medium flow, and is withdrawn as a gaseous pressure product, and wherein, in an emergency operation: product liquid is removed from the liquid tank, is brought in the liquid condition to an increased pressure, is evaporated in an indirect heat exchange with a second heat transfer medium flow and is withdrawn as a gaseous pressure product,
  • the distillation column system of the invention may be constructed as a single-column system for the nitrogen-oxygen separation, as a two-column system (for example, as a classical Linde double-column system) or as a three-column or multicolumn system.
  • it may have further devices for obtaining other air constituents, particularly noble gases, such as argon.
  • the process of the invention can be classified as one of the internal-condensation processes. This means that, in the normal operation, at least one of the products of the distillation column system (for example, nitrogen from the single column of a single-column system, from the high-pressure column of a two- or three-column system and/or from the MDS or intermediate pressure column of a three-column system—or as an alternative on in addition.
  • the products of the distillation column system for example, nitrogen from the single column of a single-column system, from the high-pressure column of a two- or three-column system and/or from the MDS or intermediate pressure column of a three-column system—or as an alternative on in addition.
  • oxygen from the single column of a single-column system or from the MDS or intermediate pressure column of a three-column system and/or from the low-pressure column of a two-column or three-column system) is taken in liquid form from one of the columns of the three-column system or from a condenser connected with one of these columns; is brought to an increased pressure in the liquid condition; is evaporated or pseudo-evaporated (at a supercritical pressure) in an indirect heat exchange with a first heat transfer medium flow; and finally obtained as a gaseous pressure product.
  • the first heat transfer medium is frequently formed by charge air and/or nitrogen.
  • the indirect heat exchange can take place in a separate heat exchanger or in the main heat exchanger in which the cooling of the charge air also takes place.
  • European Patent Document 1074805 A1 U.S. Pat. No. 6,332,337)
  • German Patent Document DE 10213212 A1 German Patent Document 10213211 A1, European Patent Document 1357342 A1 or German Patent Document DE 10238282 A1.
  • the pressure increase in the liquid can be achieved by any known measure, for example, by means of a pump, the utilization of a hydrostatic potential, and/or the pressure build-up evaporation in a tank.
  • the term “evaporating” includes a pseudo-evaporation under a supercritical pressure.
  • the pressure to which the product liquid is pressurized can therefore also be above the critical pressure; as may the pressure of the heat transfer medium which is (pseudo)condensed against the nitrogen.
  • a third operating condition the bypass operation
  • the product fraction withdrawn in a liquid state from the distillation column system is guided past the liquid tank, is pressurized in the pump set in the liquid condition to an increased pressure, is evaporated in the indirect heat exchange with a first heat transfer medium flow and is withdrawn as a gaseous pressure product.
  • the bypass operation basically separate devices can be provided.
  • the internal condensation can also be continued during times in which the tank is not available.
  • the system can continue to supply gaseous pressure product.
  • the bypass operation can also be utilized at temporary fluctuations of the purity of the liquid product fraction from the distillation column system in order to prevent a contamination of the product stored in the liquid tank; in this case also, it may be favorable to bypass the tank in the manner according to the invention.
  • the devices for the pressure increase in the liquid condition mostly consist of pumps. In principle, it is conceivable to use a single pump. However, for reasons of redundancy, a pump set is frequently used, that is, a plurality of pumps connected in parallel. In this case, a pump set may have approximately two or three pumps with a 50% capacity respectively; in the case of three (or more) pumps, one is only held in a standby position in order to take over the task of one of the other pumps in the event of a disturbance of their operation.
  • the pump quantity delivery is generally regulated by one pump bypass respectively per individual pump, by means of which the excess quantity of pumped liquid is expanded and is returned into the liquid tank.
  • the pressure increase in the liquid condition in the normal operation is carried out in a pump set which has one or more parallel-connected individual pumps, at least one individual pump having a first pump bypass by way of which at least at times a portion of the product liquid exiting from the pump is expanded and returned into the liquid tank, and that the same pump set is utilized also in the bypass operation for the pressure increase in the liquid condition
  • it is therefore advantageous, for at least one individual pump to have, in addition to the first pump bypass, a second pump bypass by way of which in the bypass operation, at least at times, a portion of the product liquid exiting from the pump is expanded, is guided past the liquid tank and is returned to the inlet of the pump set.
  • Preferably several or all pumps of the pump set each have a first and a second pump bypass in the above-mentioned sense.
  • the invention can also be applied to multibranch distillation column systems which have a common liquid tank, as described in German Patent Application 102004006283, which is no prior publication, and the applications corresponding thereto.
  • the product fraction is introduced from two or more branches of the distillation column system into the liquid tank.
  • the liquid tank as well as the devices for the pressure increase are jointly utilized by the two or two or more branches of the distillation column system.
  • the single drawing figure schematically depicts a system constructed according to preferred embodiments of the present invention.
  • a “product fraction” 2 is withdrawn in a liquid state.
  • the distillation column system is constructed as a 2-column system with a high-pressure column and a low-pressure column, and the product fraction 2 is formed by liquid oxygen from the sump of the low-pressure column.
  • a schematically depicted control unit CU is operable to control the valves of the system to carry out the processes described herein.
  • the liquid oxygen 2 is fed through an opened valve 51 by way of a pipe 3 into a liquid tank 4 .
  • liquid oxygen 5 is withdrawn from the liquid tank (valve 52 is also opened) and is fed to a pump set 6 which consists of a single pump or of several parallel-connected individual pumps.
  • the liquid is brought to approximately the desired product pressure and is guided by way the pipe 7 (valve 53 open) to a first evaporator 8 , and is evaporated there against a “first heat transfer medium flow”.
  • the latter is preferably formed by a correspondingly highly condensed flow of charge air for the air separation system 1 , or by a high-pressure nitrogen from the air separation system 1 .
  • the evaporator 8 is formed by the main heat exchanger of the air separation system 1 , in which is charge air is cooled to the fractionating temperature.
  • it can also be constructed as a heat exchanger, such as a secondary condenser, separated from the main heat exchanger.
  • oxygen exits as a gaseous pressure product and can be fed to a consuming device or a distributing system.
  • a pump bypass 10 is used for regulating the pumped quantity.
  • a throttle valve 54 as a rule, a portion of the pumped quantity is returned into the liquid tank 4 . Only one pump bypass 10 is illustrated in the drawing. If the pump set 6 consists of more than a single pump, each individual pump has a separate pipe with a separate throttle valve and shut-off valve.
  • the air separation system 1 fails as a result of a planned or unplanned operational interruption, the system is switched to an emergency operation.
  • valves 51 and 53 are closed and valve 61 is opened.
  • liquid oxygen stored in the liquid tank 4 flows by way of a pipe 60 to a second evaporator 62 which evaporates by means of a “second heat transfer medium flow” which differs from the first heat transfer medium flow.
  • the second evaporator 62 is constructed, for example, as an atmospheric evaporator or as a water bath evaporator.
  • oxygen leaves the system as a gaseous pressure product by way of the pipe 63 and is guided to a consuming device or a distributing system.

Landscapes

  • 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)
US11/205,035 2004-08-17 2005-08-17 Process and system for obtaining a gaseous pressure product by the cryogenic separation of air Abandoned US20060037357A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102004039839.9 2004-08-17
DE102004039839 2004-08-17

Publications (1)

Publication Number Publication Date
US20060037357A1 true US20060037357A1 (en) 2006-02-23

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ID=35768639

Family Applications (1)

Application Number Title Priority Date Filing Date
US11/205,035 Abandoned US20060037357A1 (en) 2004-08-17 2005-08-17 Process and system for obtaining a gaseous pressure product by the cryogenic separation of air

Country Status (5)

Country Link
US (1) US20060037357A1 (de)
CN (1) CN1737476A (de)
CA (1) CA2515980A1 (de)
DE (1) DE102005029274A1 (de)
FR (1) FR2874423A1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3010511A1 (fr) * 2013-09-10 2015-03-13 Air Liquide Procede et appareil de separation d'un melange gazeux a temperature subambiante

Families Citing this family (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009034979A1 (de) 2009-04-28 2010-11-04 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff
EP2312248A1 (de) 2009-10-07 2011-04-20 Linde Aktiengesellschaft Verfahren und Vorrichtung Gewinnung von Drucksauerstoff und Krypton/Xenon
US9400135B2 (en) * 2010-07-05 2016-07-26 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
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2520886A1 (de) 2011-05-05 2012-11-07 Linde AG Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102011112909A1 (de) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
EP2600090B1 (de) 2011-12-01 2014-07-16 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2784420A1 (de) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Verfahren zur Luftzerlegung und Luftzerlegungsanlage
WO2014154339A2 (de) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Verfahren zur luftzerlegung und luftzerlegungsanlage
EP2801777A1 (de) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Luftzerlegungsanlage mit Hauptverdichterantrieb
EP3044522A2 (de) * 2013-09-10 2016-07-20 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und vorrichtung zur trennung bei temperaturen unter der umgebungstemperatur
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
EP2963369B1 (de) 2014-07-05 2018-05-02 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
PL2963370T3 (pl) 2014-07-05 2018-11-30 Linde Aktiengesellschaft Sposób i urządzenie do kriogenicznego rozdziału powietrza
EP2963367A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch
TR201808162T4 (tr) 2014-07-05 2018-07-23 Linde Ag Havanın düşük sıcaklıkta ayrıştırılması vasıtasıyla bir basınçlı gaz ürününün kazanılmasına yönelik yöntem ve cihaz.
FR3033395A1 (fr) * 2015-03-05 2016-09-09 Air Liquide Procede et appareil de compression d’un gaz

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3668078A (en) * 1969-04-25 1972-06-06 Phillips Petroleum Co Fractional distillation bypass control process
US5505052A (en) * 1993-06-07 1996-04-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
US6038885A (en) * 1997-07-30 2000-03-21 Linde Aktiengesellschaft Air separation process
US20060010909A1 (en) * 2004-07-14 2006-01-19 Alain Briglia Backup system and method for production of pressurized gas

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3668078A (en) * 1969-04-25 1972-06-06 Phillips Petroleum Co Fractional distillation bypass control process
US5505052A (en) * 1993-06-07 1996-04-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
US6038885A (en) * 1997-07-30 2000-03-21 Linde Aktiengesellschaft Air separation process
US20060010909A1 (en) * 2004-07-14 2006-01-19 Alain Briglia Backup system and method for production of pressurized gas

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3010511A1 (fr) * 2013-09-10 2015-03-13 Air Liquide Procede et appareil de separation d'un melange gazeux a temperature subambiante
WO2015036673A3 (fr) * 2013-09-10 2015-08-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'un mélange gazeux à température subambiante

Also Published As

Publication number Publication date
FR2874423A1 (fr) 2006-02-24
CN1737476A (zh) 2006-02-22
CA2515980A1 (en) 2006-02-17
DE102005029274A1 (de) 2006-02-23

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