EP1300640A1 - Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air - Google Patents

Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air Download PDF

Info

Publication number
EP1300640A1
EP1300640A1 EP02022022A EP02022022A EP1300640A1 EP 1300640 A1 EP1300640 A1 EP 1300640A1 EP 02022022 A EP02022022 A EP 02022022A EP 02022022 A EP02022022 A EP 02022022A EP 1300640 A1 EP1300640 A1 EP 1300640A1
Authority
EP
European Patent Office
Prior art keywords
pressure column
low
nitrogen
refrigerant
low pressure
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.)
Withdrawn
Application number
EP02022022A
Other languages
German (de)
English (en)
Inventor
Stefan Lochner
Ralph Spöri
Michael Lauter
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
Priority claimed from DE10148818A external-priority patent/DE10148818A1/de
Priority claimed from DE2001148820 external-priority patent/DE10148820A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP1300640A1 publication Critical patent/EP1300640A1/fr
Withdrawn legal-status Critical Current

Links

Images

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
    • F25J3/04412—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 in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • F25J3/04284—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
    • F25J3/04763—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
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
    • F25J2215/44—Ultra high purity nitrogen, i.e. generally less than 1 ppb impurities
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/42—Separating low boiling, i.e. more volatile components from nitrogen, e.g. He, H2, Ne
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system

Definitions

  • the invention relates to a method for the production of nitrogen by Cryogenic decomposition of air in a rectification system containing a pressure column and having a low pressure column, wherein in the process feed air into the pressure column introduced, an oxygen-containing liquid fraction removed from the pressure column and is fed into the low-pressure column, gaseous nitrogen above a Mass transfer section, the at least one theoretical or has practical floor, deducted from the low pressure column and in one Top condenser by indirect heat exchange with a refrigerant at least is partially condensed and high purity nitrogen below the Removed mass transfer section from the low pressure column and as Nitrogen product is recovered.
  • the invention is based on the object, a method of the type mentioned and to provide a corresponding device that economically particularly favorable are.
  • the method is a refrigeration feed system in which a refrigerant fluid flows and at least a portion of the refrigerant fluid from the Refrigeration supply system above the mass transfer section in the low pressure column is initiated.
  • a refrigerant fluid flows and at least a portion of the refrigerant fluid from the Refrigeration supply system above the mass transfer section in the low pressure column is initiated.
  • an introduction is within the scope of the invention the refrigerant fluid from the refrigeration supply system in the upper region of the pressure column possible.
  • the refrigerant fluid can be formed in the invention by a readily available medium be introduced into the low pressure column and thus the mass transfer involved in the low-pressure column without affecting the purity of the highly pure Nitrogen product is affected and without the operating pressure of the Low pressure column can be tailored to the needs of the refrigeration system got to.
  • a suitable cryogenic fluid is nitrogen, which is still Contains volatile contaminants.
  • a residual fraction for example from Evaporation space of the top condenser, deducted, working to about Atmospheric pressure is released and removed from the process. This is the minimum operating pressure the top condenser and thus that of the low pressure column alone through the cold supply system. This disadvantage is in the invention avoided without reducing product purity.
  • the refrigerant fluid is in the invention preferably at the top of the low pressure column fed.
  • the refrigerant fluid from the pressure column removed, in the refrigeration supply system work performing relaxed and in the Low pressure column initiated.
  • the Refrigerant fluid is preferably upstream of its work-performing expansion in Indirect heat exchange against cooled process streams warmed up.
  • the mass transfer section is separated by one or more rectification plates (see above) mentioned floors) - this is the indication in "practical" number of shelves - or by a short packing section ("theoretical" number of plates).
  • the number of For example, barrier floors or theoretical floors amounts to 1 to 10, preferably 2 to 3.
  • the refrigerant fluid is usually lighter than nitrogen volatile components. Thanks to the Infeed above the described mass transfer section get this but not in the further withdrawn nitrogen product.
  • cooling fluid from the upper region of the pressure column is removed. It is characterized by a nitrogen-rich gas fraction from the Pressure column formed, in particular by the head gas.
  • the cooling fluid is passed through a deep-cold Liquid formed outside the rectification system.
  • the cryogenic liquid can be, for example, by liquid nitrogen formed from another air separation plant; Altematively can any other mixture of air components can be used.
  • the external one Liquid can either be introduced via a pipeline or from a Storage tanks are removed. The feed takes place at the point that the composition of the external fluid corresponds. This can be the top one Be the area of the pressure or low pressure column.
  • the cryogenic liquid may partially or completely enter the low pressure column are introduced, preferably at the head.
  • the deep cold liquid at least partially in the upper part of the pressure column be introduced.
  • refrigerant for the top condenser from the bottom of the Low pressure column removed, and the entire oxygenated product of Pressure column is fed into the low pressure column.
  • oxygenated here every fraction is understood, whose oxygen content is greater than that of the air is.
  • the nitrogen product can be withdrawn in gaseous form from the low pressure column. Alternatively, it is taken from the low-pressure column in liquid and in indirect Heat exchange with work-performing expanded refrigerant fluid evaporates. Also one Combination of these two process steps is possible.
  • the invention also relates to a device according to claims 10 to 12th
  • Compressed and purified air 1 is cooled in the embodiment of Figure 1 in a main heat exchanger 2 and a pressure column 4 under a pressure of 9 to 13 bar supplied (3).
  • the rectification system also has a low-pressure column 5 which is operated at a pressure of 2 to 5 bar and is in heat-exchanging communication with the pressure column via a common condenser-evaporator (main condenser) 6.
  • Part 8 of the nitrogen withdrawn at the top of the pressure column is liquefied in the main condenser 6 and partly fed via lines 9 and 10 as reflux to the pressure column.
  • Another stream 14 of the liquid 9 from the main condenser 6 is subcooled (15) and fed to a first part 20 as reflux of the low pressure column 5 at the top.
  • To a second part 21 of the supercooled nitrogen is withdrawn as a liquid product PLIN.
  • Bottom liquid 11 of the pressure column is throttled after supercooling 15 as an oxygen-containing liquid fraction in the low-pressure column 5 (12).
  • the bottom liquid 13 of the low-pressure column 5 is also undercooled (15) and relaxed (16) and then into the evaporation space of the top condenser 17th introduced the low pressure column 5. Condensed in the liquefaction space gaseous nitrogen 18 from the top of the low-pressure column 5; the condensate 19 is in the low pressure column returned and used there as an additional return. Out the lower portion of the evaporation space of the top condenser 17 is over Line 22 continuously or intermittently a flushing fluid (PURGE) deducted.
  • PURGE flushing fluid
  • the generated in the top condenser 17 steam 23 is in the heat exchanger 15 and the second warmed to about ambient temperature and discarded via line 24 and / or as a regeneration gas for a cleaning device, not shown (for example Molecular sieve station) used. Via a line 35 is not condensed gas, which in particular contains more volatile components, deducted. It will blown off (36) and / or admixed with the steam 23 (37).
  • a mass transfer section 25 which in the example is formed by three practical floors (barrier floors).
  • gaseous nitrogen via line 26 as a highly pure product taken and in the heat exchanger 15 and 2 to about ambient temperature warmed up.
  • the warm nitrogen product 27 can be used immediately as a final product (PGAN) be used or it is - as shown in the drawing - first in one Nitrogen compressor 28 with aftercooler 29 further compressed and finally over Deducted line 30.
  • cryogenic liquid from outside the rectification system into one of the columns of the Rectification is initiated
  • Liquid Assist a cryogenic liquid from outside the rectification system into one of the columns of the Rectification is initiated
  • the cryogenic Liquid may not necessarily have been generated outside the rectification system; rather, liquid can also be used for emergency operation (for example, liquid nitrogen) used during normal operation of the plant and in one Storage tank is stored.
  • the embodiment of Figure 1 can be modified so that in the Low pressure column, a gaseous and / or liquid oxygen product is generated.
  • a gaseous and / or liquid oxygen product is generated.
  • the feed 16 of bottoms of the Low pressure column in this evaporation space is omitted in whole or in part. From the Sump area of the low-pressure column 5, the oxygen product is gaseous and / or withdrawn liquid.
  • Compressed and cleaned air 1 is cooled in the embodiment of Figure 2 in a main heat exchanger 2 and a pressure column 4 under a pressure of 9 to 10 bar supplied (3).
  • the rectification system also has a low-pressure column 5 which is operated at a pressure of 2 to 3 bar and is in heat-exchanging communication with the pressure column via a common condenser-evaporator (main condenser) 6.
  • the withdrawn at the top of the pressure column nitrogen 8 is liquefied in the main condenser 6 and partially abandoned via lines 9 and 10 as reflux to the pressure column.
  • Another part 14 of the liquid 9 from the main condenser 6 is subcooled (15) and fed to a first part 20 as reflux of the low pressure column 5 at the top.
  • To a second part 21 of the supercooled nitrogen is withdrawn as a liquid product PLIN.
  • Bottom liquid 11 of the pressure column is throttled after supercooling 15 as an oxygen-containing liquid fraction in the low-pressure column 5 (12).
  • the bottom liquid 13 of the low-pressure column 5 is also undercooled (15) and relaxed (16) and then into the evaporation space of the top condenser 17th introduced the low pressure column 5. Condensed in the liquefaction space gaseous nitrogen 18 from the top of the low-pressure column 5; the condensate 19 is in the low pressure column returned and used there as an additional return. Out the lower portion of the evaporation space of the top condenser 17 is over Line 22 continuously or intermittently a flushing fluid (PURGE) deducted.
  • PURGE flushing fluid
  • the generated in the top condenser 17 steam 23 is in the heat exchanger 15 and the second warmed to about ambient temperature and discarded via line 24 and / or as a regeneration gas for a cleaning device, not shown (for example Molecular sieve station) used. Via a line 35 is not condensed gas, which in particular contains more volatile components, deducted. It will blown off (36) and / or admixed with the steam 23 (37).
  • a mass transfer section 25 which in the example is formed by three practical floors (barrier floors).
  • gaseous nitrogen via line 26 as a highly pure product taken and in the heat exchanger 15 and 2 to about ambient temperature warmed up.
  • the warm nitrogen product 27 can be used immediately as a final product (PGAN) be used or it is - as shown in the drawing - first in one Nitrogen compressor 28 with aftercooler 29 further compressed and finally over Deducted line 30.
  • liquid nitrogen from the storage tank 39 as a refrigerant fluid in the Pressure column are fed (not in the drawing ) Shown.
  • the embodiment of Figure 2 can be modified so that in the Low pressure column, a gaseous and / or liquid oxygen product is generated.
  • a gaseous and / or liquid oxygen product is generated.
  • the feed 16 of bottoms of the Low pressure column in this evaporation space is omitted in whole or in part. From the Sump area of the low-pressure column 5, the oxygen product is gaseous and / or withdrawn liquid.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP02022022A 2001-10-04 2002-10-01 Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air Withdrawn EP1300640A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE10148818 2001-10-04
DE10148818A DE10148818A1 (de) 2001-10-04 2001-10-04 Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft
DE2001148820 DE10148820A1 (de) 2001-10-04 2001-10-04 Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft
DE10148820 2001-10-04

Publications (1)

Publication Number Publication Date
EP1300640A1 true EP1300640A1 (fr) 2003-04-09

Family

ID=26010289

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02022022A Withdrawn EP1300640A1 (fr) 2001-10-04 2002-10-01 Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air

Country Status (3)

Country Link
US (1) US6708523B2 (fr)
EP (1) EP1300640A1 (fr)
CN (1) CN100334412C (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1903290A4 (fr) * 2005-06-23 2011-02-16 Air Water Inc Dispositif de production d'azote et appareil d'utilisation associé

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102005010054A1 (de) * 2005-03-04 2006-09-07 Linde Ag Verfahren zum gleichzeitigen Gewinnen einer Helium- und einer Stickstoff-Reinfraktion
FR2895069B1 (fr) * 2005-12-20 2014-01-31 Air Liquide Appareil de separation d'air par distillation cryogenique
US20130000351A1 (en) * 2011-06-28 2013-01-03 Air Liquide Process & Construction, Inc. Production Of High-Pressure Gaseous Nitrogen
US9097459B2 (en) * 2011-08-17 2015-08-04 Air Liquide Process & Construction, Inc. Production of high-pressure gaseous nitrogen
CN102506559A (zh) * 2011-09-28 2012-06-20 开封东京空分集团有限公司 多段精馏制取高纯氮气空分工艺
CN102589250A (zh) * 2012-02-14 2012-07-18 开封黄河空分集团有限公司 一种由空气分离制取氮气的工艺
EP2634517B1 (fr) * 2012-02-29 2018-04-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et appareil pour la séparation d'air par distillation cryogénique
CN108692524B (zh) * 2018-04-18 2020-06-09 衢州杭氧气体有限公司 一种工业氧、氮气生产工艺及其生产线

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4717410A (en) * 1985-03-11 1988-01-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for producing nitrogen under pressure
US5137559A (en) * 1990-08-06 1992-08-11 Air Products And Chemicals, Inc. Production of nitrogen free of light impurities
EP0539268A1 (fr) * 1991-10-15 1993-04-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé d'élimination d'hydrogène par distillation cryongénique en vue d'obtenir de l'azote à grande pureté
US5964104A (en) * 1997-05-15 1999-10-12 Linde Aktiengesellschaft Method and device for obtaining nitrogen by low-temperature separation of air
EP0955509A1 (fr) * 1998-04-30 1999-11-10 Linde Aktiengesellschaft Procédé et appareil pour la production d'oxygène à haute pureté

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1025067C (zh) * 1989-02-23 1994-06-15 琳德股份公司 精馏分离空气的方法及装置
DE19735154A1 (de) 1996-10-30 1998-05-07 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff
GB9711258D0 (en) * 1997-05-30 1997-07-30 Boc Group Plc Air separation
JP3719832B2 (ja) * 1997-10-14 2005-11-24 日本エア・リキード株式会社 超高純度窒素及び酸素の製造装置
DE19921949A1 (de) * 1999-05-12 2000-11-16 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4717410A (en) * 1985-03-11 1988-01-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for producing nitrogen under pressure
US5137559A (en) * 1990-08-06 1992-08-11 Air Products And Chemicals, Inc. Production of nitrogen free of light impurities
EP0539268A1 (fr) * 1991-10-15 1993-04-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé d'élimination d'hydrogène par distillation cryongénique en vue d'obtenir de l'azote à grande pureté
US5964104A (en) * 1997-05-15 1999-10-12 Linde Aktiengesellschaft Method and device for obtaining nitrogen by low-temperature separation of air
EP0955509A1 (fr) * 1998-04-30 1999-11-10 Linde Aktiengesellschaft Procédé et appareil pour la production d'oxygène à haute pureté

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1903290A4 (fr) * 2005-06-23 2011-02-16 Air Water Inc Dispositif de production d'azote et appareil d'utilisation associé
US8549878B2 (en) 2005-06-23 2013-10-08 Air Water Inc. Method of generating nitrogen and apparatus for use in the same

Also Published As

Publication number Publication date
US20030079499A1 (en) 2003-05-01
CN1423108A (zh) 2003-06-11
US6708523B2 (en) 2004-03-23
CN100334412C (zh) 2007-08-29

Similar Documents

Publication Publication Date Title
EP2235460B1 (fr) Procédé et installation pour la séparation cryogénique d'air
EP1067345B1 (fr) Procédé et dispositif pour la séparation cryogénique des constituants de l'air
EP3870915B1 (fr) Procédé et installation de séparation d'air à basse température
EP1357342B1 (fr) Système de séparation d'air cryogénique à trois colonnes avec production d'argon
EP0948730B1 (fr) Procede et dispositif de production d'azote comprime
EP1376037B1 (fr) Procédé et dispositif de séparation d'air avec une colonne de mélange et récupération de krypton et xénon
EP0955509A1 (fr) Procédé et appareil pour la production d'oxygène à haute pureté
DE69301557T2 (de) Hybrider Luft und Stickstoff Kreislaufverflüssiger
EP1666824A1 (fr) Procédé et dispositif pour la récupération d'Argon par séparation cryogénique d'air
DE19954593A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE10332863A1 (de) Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft
WO2021078405A1 (fr) Procédé et système pour la séparation d'air à basse température
EP3980705A1 (fr) Procédé et installation de décomposition d'air à basse température
EP2551619A1 (fr) Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air
DE19933558C5 (de) Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
EP4065910A1 (fr) Procédé et installation pour fractionnement à basse température de l'air
DE10153919A1 (de) Verfahren und Vorrichtung zur Gewinnung hoch reinen Sauerstoffs aus weniger reinem Sauerstoff
DE202009004099U1 (de) Vorrichtung zur Tieftemperaturzerlegung von Luft
WO2014067662A2 (fr) Procédé de séparation d'air à basse température dans une installation de séparation d'air et installation de séparation d'air
DE10045128A1 (de) Verfahren und Vorrichtung zur Erzeugung hoch reinen Stickstoffs durch Tieftemperatur-Luftzerlegung
DE20319823U1 (de) Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung
DE102016015446A1 (de) Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage
EP1001236A2 (fr) Procédé de production d'azote à ultra haute pureté
DE19543395A1 (de) Doppelsäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
DE202018006161U1 (de) Anlage zur Tieftemperaturzerlegung von Luft

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

AX Request for extension of the european patent

Extension state: AL LT LV MK RO SI

17P Request for examination filed

Effective date: 20030822

AKX Designation fees paid

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: LINDE AKTIENGESELLSCHAFT

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: LINDE AG

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20090505