EP1582830A1 - Verfahren und Apparatus zur Tieftemperaturluftzerlegung - Google Patents

Verfahren und Apparatus zur Tieftemperaturluftzerlegung Download PDF

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Publication number
EP1582830A1
EP1582830A1 EP04251844A EP04251844A EP1582830A1 EP 1582830 A1 EP1582830 A1 EP 1582830A1 EP 04251844 A EP04251844 A EP 04251844A EP 04251844 A EP04251844 A EP 04251844A EP 1582830 A1 EP1582830 A1 EP 1582830A1
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EP
European Patent Office
Prior art keywords
column
lox
air
vapour
reboiler
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.)
Ceased
Application number
EP04251844A
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English (en)
French (fr)
Inventor
Alan Linsday Prentice
Declan Patrick O'connor
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.)
Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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 Air Products and Chemicals Inc filed Critical Air Products and Chemicals Inc
Priority to EP04251844A priority Critical patent/EP1582830A1/de
Priority to US11/083,451 priority patent/US20050210916A1/en
Priority to CN200510068588.5A priority patent/CN1677040A/zh
Publication of EP1582830A1 publication Critical patent/EP1582830A1/de
Ceased 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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04418—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system with thermally overlapping high and low pressure columns
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04424—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system without thermally coupled high and low pressure columns, i.e. a so-called split columns
    • 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—Oxygen

Definitions

  • the present invention relates generally to the cryogenic separation of air into gaseous nitrogen (“GAN”) and gaseous oxygen (“GOX”) and, in particular but not necessarily exclusively, it relates to the production of GOX at low pressure and low purity.
  • GAN gaseous nitrogen
  • GOX gaseous oxygen
  • VSA vacuum swing absorption
  • US-A-5408831 (Guillard et al ) and US-A-5505052 (Ekins et al ) both disclose single reboiler/condenser cycles for the production of GOX in which at least a portion of the refrigeration duty for the processes is provided by at least one refrigerant from an external source.
  • LOX liquid oxygen
  • LIN liquid nitrogen
  • LAR liquid argon
  • US-A-6539748 discloses the use of LOX from an external source to provide refrigeration in a single reboiler/condenser cycle process for the production of low purity GOX.
  • a stream of LOX refrigerant from an external source is injected into the main heat exchanger at a pressure greater than that of the LOX entering the main heat exchanger from the distillation system.
  • the resultant vaporised LOX refrigerant is then combined with the vaporised LOX taken from the distillation system to provide a combined GOX product.
  • Low pressure GOX may be produced in a double cryogenic distillation column system using a dual reboiler/condenser cycle.
  • Examples of existing dual reboiler/condenser cycle processes are disclosed in US-A-3210951 (Gaumer), US-A-4410343 (Ziemer) and US-A-4702757 (Kleinberg). The processes disclosed in each of these references produce refrigeration by expansion of a process stream.
  • Air is compressed in an air compressor 10 to produce a stream 12 of compressed air which is then purified in a temperature swing absorption purifier 14 to produce a stream 16 of purified compressed air.
  • Stream 16 is then divided into two portions.
  • the first portion 18 is further compressed in a compressor 20 and then fed as stream 21 to the warm end of the main heat exchanger 22 where it is condensed by indirect heat exchange against vaporising LOX to produce a stream 24 of liquid air (“LAIR").
  • the LAIR is then fed to the lower pressure (“LP") column 26 of the distillation system where it is separated into nitrogen overhead and LOX.
  • a stream 28 of LOX is removed and fed to the cold end of the main heat exchanger 22 where it is vaporised by indirect heat exchange against the feed air to produce a stream 30 of low pressure GOX.
  • the second portion 32 is fed to the warm end of the main heat exchanger 22 where it is cooled by indirect heat exchange against vaporising LOX to produce a stream 34 of cooled compressed feed air.
  • a stream 35 of gaseous nitrogen (“GAN”) is removed from the LP column 26 and warmed in the main heat exchanger 22 to produce a stream 37 of waste GAN.
  • stream 34 is divided into two parts, the first part 36 is divided into two substreams.
  • the first substream 38 is fed to the higher pressure (“HP") column 40 of the distillation column system at a high pressure for separation into nitrogen-rich overhead vapour and crude liquid oxygen (“CLOX").
  • the second substream 42 is partially condensed in a first reboiler/condenser 44 located in the sump of the LP column 26 to produce a stream 46 of partially condensed air which is then fed to the bottom of the HP column 40.
  • a stream 48 of nitrogen-rich overhead vapour from the HP column 40 is condensed in a second reboiler/condenser 50 against vaporising CLOX removed via stream 52 from the HP column 40.
  • the condensed nitrogen-rich overhead is fed as streams 54 and 56 to the HP column 40 and LP column 26 respectively to provide reflux for the separations.
  • Vaporised CLOX is fed via stream 58 to the LP column 26.
  • Refrigeration for the process is provided by an expansion turbine 60.
  • the second part 62 of the cooled compressed air is fed to the expander 60 where it is work expanded to produce a stream 64 of expanded air that is then fed to the LP column 26.
  • the expander sends part of the medium pressure air directly to the LP column 26, it reduces the air flow available to the HP column 40 and the second reboiler/condenser 50. Consequentially, distillation is impaired with reduced boil-up of LOX in the sump of the LP column 26 and reduced reflux down the LP column 26.
  • the benefit of the dual reboiler/condenser cycle is that high pressure air is at a lower pressure than in a conventional cycle as LOX in the LP column 26 is vaporised by condensing air rather than nitrogen. This difference in air pressure results in reduced power unless the air flow to produce a given flow of GOX increases.
  • the effect of impaired distillation is to increase the air flow and hence the power advantage of the dual reboiler/condenser cycle with an expander is small when compared to a conventional cycle and unlikely to be sufficient to justify the additional complexity and cost of this cycle.
  • One objective of preferred embodiments of the present invention is to provide a process and apparatus for the production of low pressure GOX, in particular at low purity, with reduced power consumption (and, thus, with reduced operating cost) without any significant increase in capital cost.
  • a process for cryogenically separating air in a cryogenic distillation system comprising a higher pressure (“HP") distillation column and a lower pressure (“LP”) distillation column, a first reboiler/condenser, a second reboiler/condenser and heat exchange means, said process comprising:
  • One advantage of preferred embodiments of the present invention is that it is not necessary to provide refrigeration for the process by expansion of a process stream.
  • the use of an expander incurs significant capital and operational cost and can increase energy consumption.
  • the overall refrigeration requirement of the process is met without expansion of a process stream thereby eliminating these penalties in cost and energy consumption.
  • the liquid and vapour flow in the HP column is increased, compared to prior art processes having expanders.
  • the increase in air flow in the present invention is substantially zero when compared to the air flow in a conventional single reboiler/condenser cycle.
  • the or each refrigerant may be introduced into any suitable location in the cryogenic section of the plant.
  • the or at least one refrigerant is LOX
  • at least a portion of the required refrigeration duty for the process may be provided by feeding LOX from an external source to the sump of the LP column.
  • at least a portion of the required refrigeration duty for the process may be provided by vaporising LOX from an external source by indirect heat exchange against compressed air in the heat exchange means to produce cooled compressed air and vaporised refrigerant. It would also be possible to provide at least a portion of the refrigeration duty by carrying out both of these steps in combination.
  • LOX refrigerant is vaporised in the main exchange means
  • the resultant GOX may be combined with the GOX produced by vaporising LOX from the LP column to produce combined GOX product.
  • LIN from an external source may be introduced into the distillation column system at a location having a high nitrogen concentration.
  • LIN from an external source may be fed to the top of the LP column, the top of the HP column or to the top of both columns.
  • Both LIN and LOX from external sources may be used simultaneously to provide at least a portion of the refrigeration duty required by the process. However, in preferred embodiments, only one refrigerant is used.
  • the first reboiler/condenser is usually located in the sump of the LP column.
  • the process comprises at least partially condensing air by indirect heat exchange against LOX produced in the LP column to produce said oxygen vapour and said at least partially condensed air.
  • the second reboiler/condenser may be located at an intermediate location in the LP column in which case the process comprises at least partially condensing the nitrogen-rich overhead vapour by indirect heat exchange against oxygen-rich liquid descending the LP column to produce said oxygen-rich vapour and said at least partially condensed nitrogen-rich overhead vapour.
  • the second reboiler/condenser may be located outside the LP column.
  • the process may comprise at least partially condensing the nitrogen-rich overhead vapour by indirect heat exchange against CLOX produced in the HP column to produce said crude oxygen vapour and said at least partially condensed nitrogen-rich overhead vapour.
  • a portion of the required refrigeration duty may be provided by expansion of a process stream. However, in preferred embodiments, there is no expansion of a process stream to provide refrigeration.
  • An advantage of these preferred embodiments is that the capital and operational costs of dual reboiler/condenser cycles may be reduced if there are no expansion turbines present in the system.
  • the feed air may comprise at least a portion of the cooled compressed air. Alternatively or additionally, the feed air may comprise at least a portion of the at least partially condensed air.
  • Feed air to the HP column is preferably cooled compressed air with LAIR being fed to the LP column.
  • the all of the cooled compressed feed air is at least partially condensed in the first reboiler/condenser and then fed to the HP column.
  • LAIR can be fed to the HP column or split between the HP and LP columns.
  • Reflux for the LP and HP columns may be provided by any suitable liquid stream in the process.
  • both the HP column and the LP column may be refluxed with at least partially condensed nitrogen-rich overhead vapour.
  • low purity GOX e.g. GOX having an oxygen concentration from about 80 to about 98 vol %, preferably about 95 vol %
  • the pressure of the GOX is preferably from about 1.5 to about 5.0 bar absolute (0.15 to 0.5 MPa). Preferably, the pressure is from about 1.7 to about 2.3 bar absolute (0.17 to 0.23 MPa). Nitrogen overhead vapour may be removed from the HP column, warmed in the main heat exchanger and collected as a GAN product.
  • apparatus for cryogenically separating air comprising:
  • the apparatus may be adapted and/or constructed to operate any of the preferred processes described above.
  • the or at least one refrigerant conduit means is adapted to carry LOX and, preferably, is in fluid flow communication with the sump of the LP column. Additionally or alternatively, the or at least one refrigerant conduit means may be in fluid flow communication with the cold end of the heat exchange means.
  • the apparatus may further comprise GOX conduit means for combining the GOX produced by vaporising LOX from the LP column and GOX produced by vaporising the LOX refrigerant.
  • the or at least one refrigerant conduit means is adapted tc carry LIN and, preferably, is in fluid flow communication with a location of the distillation system having high nitrogen concentration. Suitable examples of such loccns include the top of the LP column and the top of the HP column.
  • the first reboiler/condenser is usually located in the sump of the LP column.
  • the second reboiler/condenser may be located at an intermediate location in the LP column or may be located outside the LP column. In the latter case, the apparatus may further comprise conduit means for feeding crude oxygen vapour from the second reboiler/condenser to the LP column.
  • the apparatus may further comprise conduit means for feeding at least a portion of the partially condensed air as feed air to the HP column.
  • the apparatus may further comprise, either additionally.or alternatively, conduit means for feeding at least a portion of the cooled compressed air as feed air to the HP column.
  • the second reboiler/condenser 50 is located at an intermediate location in the LP column 26 rather than outside the LP column 26 as in the embodiment depicted in Figure 2.
  • CLOX is, therefore, fed directly to the LP column as stream 72.
  • Refrigeration is not provided by expansion of a process stream as in Figure 1.
  • a stream 66 of LOX is introduced into the cryogenic section of the plant.
  • the LOX stream 66 is vaporised in the main heat exchanger 22 by indirect heat exchange against streams 32 and 21 of compressed air to produce a stream 68 of GOX which is then combined with GOX stream 30 to produce a stream 70 of combined GOX product.
  • the compressed air stream 36 is cooled to about its dew point and the LOX stream 28 removed from the LP column 26 is pressurised either by static head or using a pump (not shown).
  • the stream 66 of LOX from an external source is fed to the sump of the LP column 26 rather than to the main heat exchanger 22 to provide refrigeration for the process.
  • the LIN stream 74 is fed from an external source to the top of the LP column 26 to provide refrigeration for the process.
  • Cycle S2 is a single reboiler cycle with imported LOX for refrigeration (i.e. no expander).
  • Cycle S3 is the same cycle as cycle S2 except it uses an expander to provide refrigeration instead of imported LOX. There is a MAC/booster power increase of over 4%.
  • Cycle D2 is a conventional dual reboiler cycle using an expander for refrigeration.
  • the MAC/booster power for this cycle is about 5% lower than observed in cycle S2.
  • Cycle D1 is a dual reboiler cycle according to the present invention (i.e. uses imported LOX rather than an expander to provide refrigeration).
  • the MAC/booster power for this cycle is about 11% lower than that for cycle S2 and about 6% lower than that for about conventional dual reboiler cycle D2.

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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)
EP04251844A 2004-03-29 2004-03-29 Verfahren und Apparatus zur Tieftemperaturluftzerlegung Ceased EP1582830A1 (de)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP04251844A EP1582830A1 (de) 2004-03-29 2004-03-29 Verfahren und Apparatus zur Tieftemperaturluftzerlegung
US11/083,451 US20050210916A1 (en) 2004-03-29 2005-03-18 Process and apparatus for the cryogenic separation of air
CN200510068588.5A CN1677040A (zh) 2004-03-29 2005-03-29 用于空气低温分离的方法和设备

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP04251844A EP1582830A1 (de) 2004-03-29 2004-03-29 Verfahren und Apparatus zur Tieftemperaturluftzerlegung

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EP1582830A1 true EP1582830A1 (de) 2005-10-05

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EP04251844A Ceased EP1582830A1 (de) 2004-03-29 2004-03-29 Verfahren und Apparatus zur Tieftemperaturluftzerlegung

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EP (1) EP1582830A1 (de)
CN (1) CN1677040A (de)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11815309B2 (en) * 2018-11-07 2023-11-14 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Integration of hydrogen liquefaction with gas processing units
US20230074304A1 (en) * 2021-09-07 2023-03-09 Uop Llc Vapor distribution system in a concentric reboiler
CN113750797A (zh) * 2021-09-15 2021-12-07 黑龙江豪运药业有限公司 低温真空精馏三氟化硼分离高丰度同位素硼11三氟化硼的装置和方法

Citations (4)

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Publication number Priority date Publication date Assignee Title
US4668260A (en) * 1984-07-13 1987-05-26 Daidousanso Co., Ltd. High-purity nitrogen gas production equipment
US5743112A (en) * 1995-11-02 1998-04-28 Teisan Kabushiki Kaisha Ultra high purity nitrogen and oxygen generator unit
US6185960B1 (en) * 1998-04-08 2001-02-13 Linde Aktiengesellschaft Process and device for the production of a pressurized gaseous product by low-temperature separation of air
US20030110796A1 (en) * 2001-12-14 2003-06-19 Linde Aktiengesellschaft Apparatus and process for producing gaseous oxygen under elevated pressure

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US3210951A (en) * 1960-08-25 1965-10-12 Air Prod & Chem Method for low temperature separation of gaseous mixtures
US4410343A (en) * 1981-12-24 1983-10-18 Union Carbide Corporation Air boiling process to produce low purity oxygen
GB2125949B (en) * 1982-08-24 1985-09-11 Air Prod & Chem Plant for producing gaseous oxygen
US4702757A (en) * 1986-08-20 1987-10-27 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4842625A (en) * 1988-04-29 1989-06-27 Air Products And Chemicals, Inc. Control method to maximize argon recovery from cryogenic air separation units
US5006137A (en) * 1990-03-09 1991-04-09 Air Products And Chemicals, Inc. Nitrogen generator with dual reboiler/condensers in the low pressure distillation column
FR2699992B1 (fr) * 1992-12-30 1995-02-10 Air Liquide Procédé et installation de production d'oxygène gazeux sous pression.
FR2706195B1 (fr) * 1993-06-07 1995-07-28 Air Liquide Procédé et unité de fourniture d'un gaz sous pression à une installation consommatrice d'un constituant de l'air.
US5761927A (en) * 1997-04-29 1998-06-09 Air Products And Chemicals, Inc. Process to produce nitrogen using a double column and three reboiler/condensers
US6009723A (en) * 1998-01-22 2000-01-04 Air Products And Chemicals, Inc. Elevated pressure air separation process with use of waste expansion for compression of a process stream
EP1207362A1 (de) * 2000-10-23 2002-05-22 Air Products And Chemicals, Inc. Verfahren und Vorrichtung zur Herstellung von gasförmigem Niederdrucksauerstoff

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4668260A (en) * 1984-07-13 1987-05-26 Daidousanso Co., Ltd. High-purity nitrogen gas production equipment
US5743112A (en) * 1995-11-02 1998-04-28 Teisan Kabushiki Kaisha Ultra high purity nitrogen and oxygen generator unit
US6185960B1 (en) * 1998-04-08 2001-02-13 Linde Aktiengesellschaft Process and device for the production of a pressurized gaseous product by low-temperature separation of air
US20030110796A1 (en) * 2001-12-14 2003-06-19 Linde Aktiengesellschaft Apparatus and process for producing gaseous oxygen under elevated pressure

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CN1677040A (zh) 2005-10-05
US20050210916A1 (en) 2005-09-29

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