EP0878677A1 - Procédé et dispositif pour la production d'azote par séparation cryogénique d'air - Google Patents

Procédé et dispositif pour la production d'azote par séparation cryogénique d'air Download PDF

Info

Publication number
EP0878677A1
EP0878677A1 EP97113507A EP97113507A EP0878677A1 EP 0878677 A1 EP0878677 A1 EP 0878677A1 EP 97113507 A EP97113507 A EP 97113507A EP 97113507 A EP97113507 A EP 97113507A EP 0878677 A1 EP0878677 A1 EP 0878677A1
Authority
EP
European Patent Office
Prior art keywords
pressure column
nitrogen gas
nitrogen
column
gas fraction
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Withdrawn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
EP97113507A
Other languages
German (de)
English (en)
Inventor
Dietrich Dipl.-Ing. Rottmann
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
Priority to DE59806495T priority Critical patent/DE59806495D1/de
Priority to ES98107748T priority patent/ES2189032T3/es
Priority to DK98107748T priority patent/DK0878678T3/da
Priority to EP19980107748 priority patent/EP0878678B1/fr
Publication of EP0878677A1 publication Critical patent/EP0878677A1/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Withdrawn legal-status Critical Current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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another 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
    • F25J3/04284—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
    • F25J3/04406—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
    • 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
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid 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
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • the invention relates to a method and an apparatus for the production of nitrogen by low-temperature separation of air by means of two-stage rectification in one Double column, which has a high pressure column and a medium pressure column, the are in heat exchange relationship with one another, with the method being air compressed, cleaned, in a main heat exchanger against decomposition products cooled and fed to the rectification, at least one nitrogen product fraction discharged from the high pressure column and a nitrogen gas fraction the double column warmed up, relaxed and at least partly in indirect Heat exchange with an oxygen-enriched liquid from the bottom Area of the medium pressure column is brought, the nitrogen gas fraction at least partially condensed and the oxygen-enriched liquid at least partially is evaporated, and which is formed in the indirect heat exchange Condensate is at least partially returned to the medium pressure column.
  • the invention is therefore based on the object of such a method and specify appropriate device, which is characterized by particularly high Profitability, in particular through low energy consumption and / or low Mark apparatus costs.
  • This object is achieved in that the nitrogen gas fraction upstream of the Relaxation is warmed to an intermediate temperature between the Temperatures at the cold and warm end of the main heat exchanger.
  • the heating of the nitrogen gas fraction is regularly caused by indirect Heat exchange causes.
  • it can be in the main heat exchanger be carried out, which is used to cool the feed air.
  • the measure according to the invention is omitted at least in part by heating the Nitrogen gas fraction from the intermediate temperature to the warm temperature End of the main heat exchanger (usually about the same as the ambient temperature) and the corresponding re-cooling. They are correspondingly lower Exchange losses in the corresponding heat exchanger, which means less is possible Energy lost through irreversibility.
  • the corresponding heat exchanger can also have fewer passages and are therefore cheaper to produce will.
  • the intermediate temperature to which the nitrogen gas fraction is heated is for example 140 to 190 K below the temperature of the warm end of the Main heat exchanger.
  • the relaxation of the nitrogen gas fraction upstream of it Condensation through indirect heat exchange preferably leads to one Intermediate pressure between the pressures of the high pressure column and the medium pressure column or to a pressure below the medium pressure column pressure. Accordingly, the Pressure of the condensate reduced before introduction into the medium pressure column or can be increased, for example by a throttle valve or by a Pump.
  • the nitrogen gas fraction between the heating to a The intermediate temperature and the relaxation did not cool down. This eliminates Irreversibility by heating and cooling the nitrogen gas fraction and the corresponding heat exchange devices completely.
  • the nitrogen gas fraction from the high pressure column is removed. In this case in particular, it needs between heating up to the intermediate temperature and relaxation are not compressed, so that also the corresponding machine and the associated energy consumption omitted.
  • the corresponding amount can also be considered High pressure product can be obtained from the high pressure column.
  • High pressure product can be obtained from the high pressure column.
  • Pump can be used to increase the Pressure in the condensate at the high pressure column level.
  • any known method can be used to relax the nitrogen gas fraction this relaxation is preferably carried out while performing work, for example in a turbine. Part of or all of it can be used for the Process required cold can be obtained. In addition, it is possible to use the Energy gained at least partially to compress a To use product stream, for example by mechanical coupling of the Relaxation machine to a compressor.
  • the relaxed amount of nitrogen gas fraction is so large is that it does not completely liquefy against the oxygenated liquid , it is favorable if part of the expanded nitrogen gas fraction in indirect heat exchange with an intermediate liquid from the medium pressure column is condensed.
  • the this indirect heat exchange condensate is preferably on abandoned the medium pressure column. This is due to the evaporation of the intermediate liquid
  • the resulting gas is preferably returned to the medium pressure column.
  • the additional heating of the medium pressure column thereby improves the Separation effect of this column.
  • the corresponding additional condenser evaporator can be arranged inside or outside the medium pressure column.
  • the intermediate liquid is preferably in an area below the point, at the bottom liquid from the high pressure column, and at least one, preferably 1 to 30, for example 20 theoretical plates above the Medium pressure column sump withdrawn.
  • the invention also relates to a device for producing nitrogen according to claims 9 to 12.
  • Compressed air 1 cleaned in a molecular sieve station flows through one Main heat exchanger 2 and is via line 3 in a double column 4, more precisely in whose high pressure column 5, fed.
  • Oxygenated liquid 8 from the After hypothermia 9 high pressure column 5 is fed via line 10 into the medium pressure column 6 throttled.
  • a part of the top fraction 7 of the high pressure column is through a Main capacitor 14 out, condensed there and preferably completely in again the high pressure column 5 is returned.
  • Another partial stream 17 of the top fraction 7 is led to the main heat exchanger 2.
  • the intermediate temperature is for example 175 K lower than the temperature at the warm end of the Main heat exchanger 2 (approximately the same ambient temperature).
  • the liquid in the sump of the medium pressure column 6 enters through the main condenser 14 Heat exchange with the condensing top fraction of the high pressure column.
  • From the Medium pressure column 6 are an oxygen-enriched liquid 11, a gaseous one Nitrogen stream 12 and optionally liquid nitrogen 13 removed.
  • Of the gaseous nitrogen flow is via the lines 18a and 18b and through the Heat exchanger 9, 31 and 2 out. He can from line 19a under about Subtracted ambient temperature as a medium pressure product or - as in the drawing shown - brought to a further increased product pressure in a compressor 22 and be discharged as a further high-pressure product 19b.
  • the nitrogen gas fraction is according to the invention at an intermediate temperature from the Main heat exchanger 2 removed (line 20) and then in one Relaxation machine (for example a turbine) 23 relaxed to perform work. After cooling in the heat exchanger 31, the nitrogen gas fraction 24 is in the Liquefaction chamber of a condenser-evaporator 25 initiated. There she enters indirect heat exchange with possibly supercooled in 9 oxygen-enriched liquid 28 from the sump of the medium pressure column, which evaporated, withdrawn via line 29 and preferably for the regeneration of Mol sieve station is used. The pressure on the evaporation side of the Head capacitor 25 is preferably so by means of the throttle valve in line 28 set that the overpressure necessary for the regeneration of the molecular sieve is available. If necessary, the oxygen-enriched liquid can be a pump, not shown, are promoted.
  • the work obtained in the work relaxation 23 is in the example transmitted by direct mechanical coupling to a post-compressor 22 which a product stream, here nitrogen 19a from the medium pressure column, compressed.
  • another process stream can be compressed or the mechanical energy can be applied a generator or to a brake blower.
  • the pressure in the evaporation space of the top condenser 25 adjusted by means of the valve in line 28 so that after evaporation and after the passage through the heat exchanger 9 and 2 (line 29) still for the Regeneration of the molecular sieve required overpressure is present.
  • the one for evaporation the amount of nitrogen required for the oxygen-enriched liquid (Nitrogen gas fraction) is in the expansion machine 23 to a pressure brought, which is high enough to the evaporation of the oxygenated liquid against the condensing nitrogen gas fraction To ensure 24 in the top capacitor 25, and on the other hand ensures that the Refrigeration requirements for the procedure are covered.
  • Table 1 shows preferred numerical ranges and a particularly preferred concrete numerical example for the operating pressures in the method according to FIG. 1.
  • Number range example Head of the high pressure column 5 5.0 - 9.3 bar
  • 6.2 bar Head of the medium pressure column 5 1.5 - 4.35 bar 2.9 bar
  • Entry of relaxation machine 23 4.3 - 9.9 bar
  • Exit relaxation machine 23 3.0 - 6.0 bar 4.37 bar
  • Evaporation side of the condenser-evaporator 25 1.0 - 3.0 bar 1.30 bar
  • FIG. 2 shows a modification of the method and the device according to FIG. 1. Corresponding features of the two examples have the same reference numerals. In the following, only the different features of the in FIG. 2 are described process described in detail.
  • the condensate 203 is on the top of the Medium pressure column 6 abandoned.

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)
EP97113507A 1997-05-15 1997-08-05 Procédé et dispositif pour la production d'azote par séparation cryogénique d'air Withdrawn EP0878677A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
DE59806495T DE59806495D1 (de) 1997-05-15 1998-04-28 Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft
ES98107748T ES2189032T3 (es) 1997-05-15 1998-04-28 Proceso y aparato para la produccion de nitrogeno por fraccionamiento criogenico del aire.
DK98107748T DK0878678T3 (da) 1997-05-15 1998-04-28 Fremgangsmåde og anordning til udvinding af nitrogen ved lavtemperaturfraktionering af luft
EP19980107748 EP0878678B1 (fr) 1997-05-15 1998-04-28 Procédé et dispositif de production d'azote par séparation cryogénique d'air

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19720453A DE19720453A1 (de) 1997-05-15 1997-05-15 Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft
DE19720453 1997-05-15

Publications (1)

Publication Number Publication Date
EP0878677A1 true EP0878677A1 (fr) 1998-11-18

Family

ID=7829574

Family Applications (1)

Application Number Title Priority Date Filing Date
EP97113507A Withdrawn EP0878677A1 (fr) 1997-05-15 1997-08-05 Procédé et dispositif pour la production d'azote par séparation cryogénique d'air

Country Status (3)

Country Link
US (1) US5964104A (fr)
EP (1) EP0878677A1 (fr)
DE (1) DE19720453A1 (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6125656A (en) * 1999-11-03 2000-10-03 Praxair Technology, Inc. Cryogenic rectification method for producing nitrogen gas and liquid nitrogen
US6468501B1 (en) 2000-09-14 2002-10-22 Chevrontexaco Corporation Method for heteroatom lattice substitution in large and extra-large pore borosilicate zeolites
US6397631B1 (en) 2001-06-12 2002-06-04 Air Products And Chemicals, Inc. Air separation process
EP1300640A1 (fr) 2001-10-04 2003-04-09 Linde Aktiengesellschaft Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air
DE102007051184A1 (de) * 2007-10-25 2009-04-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
CN101929791B (zh) * 2010-08-19 2012-06-13 苏州制氧机有限责任公司 大产量高纯氮设备
CN101929790B (zh) * 2010-08-19 2012-07-18 苏州制氧机有限责任公司 高纯氮设备
US10018414B2 (en) * 2015-07-31 2018-07-10 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of low pressure gaseous oxygen

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2548222B1 (de) * 1975-10-28 1977-01-27 Linde Ag Verfahren und Vorrichtung zur Luftzerlegung
DE4441920C1 (de) * 1994-11-24 1996-04-04 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3018476C2 (de) * 1979-05-16 1984-10-25 Hitachi, Ltd., Tokio/Tokyo Verfahren und Anlage zur Gewinnung von gasförmigem Stickstoff
US4617036A (en) * 1985-10-29 1986-10-14 Air Products And Chemicals, Inc. Tonnage nitrogen air separation with side reboiler condenser
US4834785A (en) * 1988-06-20 1989-05-30 Air Products And Chemicals, Inc. Cryogenic nitrogen generator with nitrogen expander
FR2728663B1 (fr) * 1994-12-23 1997-01-24 Air Liquide Procede de separation d'un melange gazeux par distillation cryogenique

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2548222B1 (de) * 1975-10-28 1977-01-27 Linde Ag Verfahren und Vorrichtung zur Luftzerlegung
DE4441920C1 (de) * 1994-11-24 1996-04-04 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung

Also Published As

Publication number Publication date
US5964104A (en) 1999-10-12
DE19720453A1 (de) 1998-11-19

Similar Documents

Publication Publication Date Title
EP1067345B1 (fr) Procédé et dispositif pour la séparation cryogénique des constituants de l'air
EP1139046B1 (fr) Procédé et installation de production d'oxygène sous haute pression par séparation cryogénique de l'air
EP1284404A1 (fr) Procédé et dispositif pour la production d'un produit sous pression par séparation cryogénique de l'air
EP0093448A2 (fr) Procédé et dispositif pour obtenir de l'oxygène gazeux sous pression élevée
EP1074805B1 (fr) Procédé et dispositif pour la production d'oxygène sous pression
DE10013073A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP0948730B1 (fr) Procede et dispositif de production d'azote comprime
EP2236964A1 (fr) Procédé et dispositif de séparation de l'air à basse température
EP1146301A1 (fr) Procédé et dispositif de production d'azote à haute pression par séparation d'air
DE19609490A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE10238282A1 (de) Verfahren zur Tieftemperatur-Zerlegung von Luft
EP0768503B1 (fr) Procédé de séparation d'air à triple colonne
DE3834793A1 (de) Verfahren zur gewinnung von rohargon
EP0878677A1 (fr) Procédé et dispositif pour la production d'azote par séparation cryogénique d'air
EP0878678B1 (fr) Procédé et dispositif de production d'azote par séparation cryogénique d'air
EP1134524B1 (fr) Procédé de production d'azote gazeux
DE4441920C1 (de) Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung
DE10045128A1 (de) Verfahren und Vorrichtung zur Erzeugung hoch reinen Stickstoffs durch Tieftemperatur-Luftzerlegung
EP1189002A1 (fr) Procédé et dispositif d'obtention de produit gazeux d'une installation de séparation d'air cryogenique
EP0775881B1 (fr) Procédé et dispositif pour la récupération d'oxygène et d'azote à pression superatmosphérique
DE19819263C2 (de) Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff
EP1284403B1 (fr) Procédé et appareil de production d'oxygène par séparation d'air cryogénique
EP1050728B1 (fr) Procedé et installation de séparation des gaz de l'air à une seule colonne
DE19543395A1 (de) Doppelsäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
DE19537910A1 (de) Doppelsäulenverfahren und -vorrichtung 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 CH DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

AKX Designation fees paid
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

18W Application withdrawn

Withdrawal date: 19990727