EP1653183A1 - Procédé et dispositif pour la séparation cryogénique d'air - Google Patents

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

Info

Publication number
EP1653183A1
EP1653183A1 EP05256250A EP05256250A EP1653183A1 EP 1653183 A1 EP1653183 A1 EP 1653183A1 EP 05256250 A EP05256250 A EP 05256250A EP 05256250 A EP05256250 A EP 05256250A EP 1653183 A1 EP1653183 A1 EP 1653183A1
Authority
EP
European Patent Office
Prior art keywords
nitrogen
column
liquid
lin
rich
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Withdrawn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
EP05256250A
Other languages
German (de)
English (en)
Inventor
Paul Higginbotham
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
Original Assignee
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
Publication of EP1653183A1 publication Critical patent/EP1653183A1/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Withdrawn legal-status Critical Current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
    • F25J3/04248—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
    • F25J3/0429—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 feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
    • F25J3/04006—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
    • F25J3/04084—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 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
    • F25J3/04006—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
    • F25J3/04006—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
    • F25J3/04151—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
    • F25J3/04151—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
    • F25J3/0423—Subcooling of liquid process streams
    • 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
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • 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
    • F25J3/0429—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 feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
    • F25J3/04442—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system in a double column flowsheet with a high pressure pre-rectifier
    • 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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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

Definitions

  • the present invention relates to a process for the cryogenic distillation of air and, in particular, to the production of high purity, pressurised gaseous nitrogen (“GAN").
  • GAN pressurised gaseous nitrogen
  • High purity GAN is typically prepared in a cryogenic air distillation process operating a pumped liquid nitrogen (“LIN”) cycle.
  • LIN pumped liquid nitrogen
  • LIN taken from the distillation system is pumped to the required product pressure and vaporised in the main heat exchanger by indirect heat exchange against condensing high pressure air.
  • the resulting liquid air (“LAIR”) is fed to the column system.
  • LAIR liquid air
  • HP high pressure
  • US-A-5419137 (Sweeney et al ; published 30 th May 1995) discloses an air separation process producing high purity nitrogen using a dual distillation column system. Overhead vapour in the LP column is partially condensed by indirect heat exchange using a condenser against high purity LIN taken from the HP column. The resultant high purity GAN is removed as product but at low pressure and thus a separate nitrogen compressor is required to compress the GAN product to the required pressure.
  • the condenser is located within the top section of the LP column.
  • This reference also discloses an arrangement where the condenser is replaced with a stripping column (often referred to as a "top hat column”) in direct heat and mass transfer relationship with the LP column.
  • US-A-4433989 discloses an air separation process producing GAN using a dual column system coupled with an auxiliary distillation column.
  • auxiliary column crude liquid oxygen from the sump of the HP column is separated into nitrogen-rich overhead vapour and oxygen-enriched bottoms liquid.
  • LIN from the HP column is reduced in pressure and used as reflux to the auxiliary column.
  • the overhead nitrogen-rich vapour is taken as product and no LIN product is withdrawn from this column.
  • US-A-4433989 also discloses a further auxiliary column in which air is separated in the further auxiliary column into oxygen-rich bottoms liquid and nitrogen-rich overhead vapour.
  • the further auxiliary column is refluxed by condensing nitrogen overhead vapour by indirect heat exchange against pressurised LOX which is provided by pumping LOX taken from the LP column. Condensed overhead vapour is removed from the further auxiliary column and fed as reflux to the HP column.
  • US-A-6276171 discloses a gas turbine integrated with an air separation unit ("ASU").
  • ASU air separation unit
  • LIN is produced in the ASU, pumped and fed to a nitrogen wash column.
  • GAN is removed from the nitrogen wash column at a pressure between 8 and 25 bar (0.8 to 2.5 MPa), warmed, compressed and mixed with combustion exhaust gas from the gas turbine prior to work expansion.
  • Bottoms liquid is removed from the wash column, expanded and fed to the ASU.
  • the wash column is primarily intended to produce low purity nitrogen.
  • US-A-5596886 (Howard; published 28 th January 1997) discloses an air separation process for the production of gaseous oxygen (“GOX”) and high purity nitrogen using a dual column system coupled with an auxiliary, nitrogen-enrichment column.
  • Nitrogen-rich overhead vapour from the HP column is warmed, compressed, cooled and then fed to the auxiliary column which is refluxed with LIN.
  • Nitrogen enriched overhead vapour is taken from the auxiliary column, condensed by indirect heat exchange against LOX from the LP column to form LIN.
  • the LIN is pumped and a portion of the pumped LIN is fed to the top of the auxiliary column.
  • US-A-4790866 discloses an air separation process using a dual column system coupled with an argon column. LIN is removed from the HP column and fed, after pressure reduction, to the condenser of the argon column where it assists condensing the overhead vapour of the argon column.
  • a process for the production of pressurised gaseous nitrogen comprising; producing liquid nitrogen (“LIN”) in a cryogenic air separation unit (“ASU”); increasing the pressure of at least a portion of said LIN to produce pressurised LIN; separating a fluid having an oxygen concentration at least equal to that of air in an auxiliary cryogenic distillation column to produce nitrogen-rich overhead vapour and oxygen-enriched bottoms liquid; transferring heat and optionally mass between at least a portion of said nitrogen-rich overhead vapour and at least a portion of said pressurised LIN to produce nitrogen-rich liquid and pressurised GAN; and feeding at least a portion of said nitrogen-rich liquid as reflux to the ASU after suitable pressure adjustment.
  • ASU cryogenic air separation unit
  • nitrogen-rich means that the nitrogen content is greater than that in air.
  • nitrogen-enriched means that the nitrogen content is greater after a particular process step has taken place.
  • oxygen-rich and oxygen-enriched have analogous meanings to those given above for “nitrogen-rich” and "nitrogen-enriched”.
  • the purity of the nitrogen-rich liquid is usually less than the purity of the LIN and preferably has a purity of between about 85 mol % nitrogen to about 99 mol % nitrogen, e.g. about 95 mol % nitrogen.
  • Preferred processes of the present invention allow the production of high purity GAN at a different pressure from the column in which the high purity LIN is separated usually without the loss of oxygen recovery typically observed in conventional pumped LIN cycles in which nitrogen is boiled against condensing air.
  • Preferred processes also require fewer separation stages. For example, in embodiments where nitrogen-rich overhead vapour is condensed by indirect heat exchange against vaporising LIN, fewer stages are needed because the auxiliary column does not have to make pure LIN. In embodiments where heat and mass are transferred between LIN and nitrogen-rich overhead vapour, the top section of the auxiliary column operates at a higher reflux ratio than it would without the return stream to the ASU and thus fewer stages are needed to reach an equivalent purity level.
  • Preferred processes are also less susceptible to operating upsets than cycles in which high purity nitrogen is boiled directly in a wash column which has no return of lower purity nitrogen to the ASU.
  • the auxiliary column does not have to make pure LIN so the purity only has to be held in the column of the ASU producing the LIN.
  • the top section operates at a higher reflux ratio than it would without the return stream to the ASU, so the purity is less sensitive to operating fluctuations in the reflux ratio.
  • the operating range of nitrogen production i.e. the range of nitrogen production rates that can be supplied efficiently, for example, without having to vent excess nitrogen or feed excess air to the auxiliary column
  • the operating range of nitrogen production may also be increased and nitrogen purity can more easily be maintained in the event that the performance of the column deteriorates.
  • Nitrogen-rich liquid is used as reflux in the ASU after suitable pressure adjustment.
  • nitrogen-rich liquid is usually used as reflux in the LP column.
  • at least a portion of the oxygen-enriched liquid is also fed, possibly as reflux, to the ASU after suitable pressure adjustment or reduction.
  • at least a portion of the oxygen-rich liquid is usually fed directly to the LP column (although it may be fed to the LP column via the HP column to recover any vapour that flashes off at the HP column pressure).
  • the oxygen concentration of the fluid is at least equal to that of air.
  • the fluid may be air or oxygen-rich fluid from the ASU.
  • the fluid may be gaseous or liquid.
  • at least a portion of the liquid is usually vaporised by indirect heat exchange against a suitable process stream using a reboiler/condenser located in the sump of the auxiliary column.
  • Suitable process streams include, for example, a side stream from an LP or HP column or, if present, from an argon column, or high pressure air supplied from a side stream of a booster air compressor, a recycle nitrogen stream or a stream of air or nitrogen from the main column system that has been compressed at cryogenic temperature.
  • the pressure of LIN may be increased by static head. However, it is preferred that LIN is pumped to increase the pressure thereof.
  • Nitrogen-rich overhead vapour may be condensed by indirect or direct heat exchange against pressurised LIN.
  • Heat may be exchanged indirectly between at least a portion of said nitrogen-rich overhead vapour and at least a portion of said pressurised LIN thereby condensing said nitrogen-rich overhead vapour to produce nitrogen-rich liquid and vaporising said pressurised LIN to produce pressurised GAN.
  • heat may be exchanged indirectly using a reboiler/condenser. If the reboiler/condenser is located above the main distillation zone or section within the auxiliary column, then pressurised LIN may be passed through the reboiler/condenser thereby condensing nitrogen-rich overhead vapour surrounding the reboiler/condenser.
  • nitrogen-rich overhead vapour may be passed through the reboiler/condenser vaporising pressurised LIN surrounding the reboiler/condenser.
  • the auxiliary column usually comprises at least a main distillation zone. Heat and mass may be transferred directly between at least a portion of said nitrogen-rich overhead vapour and at least a portion of said pressurised LIN to produce nitrogen-rich liquid and pressurised GAN.
  • the auxiliary column preferably has at least a main distillation zone and vapour/liquid contact promoting means provided above the main distillation zone.
  • the process comprises contacting directly nitrogen-rich overhead vapour with pressurised LIN in the contact promoting means to produce the nitrogen-rich liquid and pressurised GAN.
  • the contact promoting means is usually a further distillation zone. In the further distillation zone, the liquid to vapour ratio is substantially above the minimum required to produce high purity nitrogen from the impure nitrogen vapour at the top of the main distillation zone. As a result, relatively few distillation stages can be used in comparison to a process that has no return of impure nitrogen liquid.
  • the auxiliary column may be refluxed using any suitable liquid such as LAIR. However, it is preferred that a portion of nitrogen-rich liquid is used to reflux the auxiliary column.
  • the ASU may comprise any suitable distillation column arrangement including a single distillation column that produces LIN.
  • the ASU is a dual column system comprising an HP distillation column and an LP distillation column, the HP column being thermally integrated with the LP column via an ASU reboiler/condenser.
  • the process further comprising:
  • a portion of the oxygen-rich bottoms liquid produced in the HP column may be used as at least a portion of the fluid after suitable pressure adjustment.
  • the oxygen-rich bottoms liquid may be pressurised by static head but is preferably pressurised using a pump.
  • the operating pressure of the auxiliary column is usually higher than the operating pressure of the LP column and preferably higher than the operating pressure of the HP column.
  • the typical operating pressure of the LP column is from about 1.2 bara (0.12 MPa) to about 4 bara (0.4 MPa) and of the HP column is from about 4 bara (0.4 MPa) to about 12 bara (1.2 MPa).
  • Preferred operating pressures are about 4.8 bara (0.48 MPa) for the HP column and about 1.3 bara (0.13 MPa) for the LP column.
  • the operating pressure of the auxiliary column may be from about 1.0 bara (0.10 MPa) to about 30 bara (3.0 MPa) and is usually from about 1.5 bara (0.15 MPa) to about 25 bara (2.5 MPa).
  • the operating pressure of the auxiliary column is about 12 bara (1.2 MPa) .
  • the pressurised GAN is usually produced at the operating pressure of the auxiliary column and is usually produced at a pressure from about 1.0 bara (0.1 MPa) to about 25 bara (2.5 MPa) and is usually of high purity, e.g. from about 99.9 mol % nitrogen to about 99.9999 mol % nitrogen, typically about 99.99 mol % nitrogen.
  • apparatus for the production of pressurised GAN comprising:
  • the transfer enabling means may be condensing means for condensing at least a portion of nitrogen-rich overhead vapour by indirect heat exchange against pressurised LIN to produce nitrogen-rich liquid and pressurised GAN.
  • the transfer enabling means may be vapour/liquid contact promoting means, e.g. a further distillation zone, for promoting direct contact between nitrogen-rich overhead vapour and pressurised LIN, the contact promoting means being located within the auxiliary distillation column above the main distillation zone.
  • the ASU may comprise a single distillation column.
  • the ASU comprises a dual distillation column system.
  • the reduced pressure nitrogen-rich liquid may be fed either to the HP column or to the LP column. It is also preferably subcooled before being reduced in pressure to minimise the formation of flash vapour.
  • the apparatus preferably further comprises pressure reducing means for reducing the pressure of oxygen-enriched liquid to produce reduced pressure oxygen-enriched liquid, conduit means for feeding oxygen-enriched liquid from the auxiliary column to the pressure reducing means and conduit means for feeding reduced pressure oxygen-enriched liquid from the pressure reducing means to the ASU, possibly as reflux.
  • pressure reducing means for reducing the pressure of oxygen-enriched liquid to produce reduced pressure oxygen-enriched liquid
  • conduit means for feeding oxygen-enriched liquid from the auxiliary column to the pressure reducing means
  • the ASU comprises a dual column system
  • the reduced pressure oxygen-enriched liquid is usually fed to the LP column, normally via the bottom of the HP column.
  • Each pressure reducing means may be any suitable means for reducing the pressure of a cryogenic liquid or gas.
  • the pressure reducing means is an expansion valve such as a Joule-Thompson valve.
  • the apparatus may be adapted and/or constructed to enable operation of any of the above-mentioned preferred process embodiments.
  • a stream 12 of air or an oxygen-rich fluid (such as oxygen-rich bottoms liquid from an HP column of a dual column ASU (not shown) following pressurisation using a pump (not shown) or a compressor (not shown) if the feed is vapour) is fed to the bottom of an auxiliary distillation column 14 where it is separated into nitrogen-rich overhead vapour and oxygen-enriched bottoms liquid.
  • an oxygen-rich fluid such as oxygen-rich bottoms liquid from an HP column of a dual column ASU (not shown) following pressurisation using a pump (not shown) or a compressor (not shown) if the feed is vapour
  • the fluid is a liquid
  • at least a portion of the liquid is vaporised by indirect heat exchange against a process stream using optional reboiler/condenser 16.
  • a stream 18 of pure LIN is taken from an ASU (not shown) and pumped in pump 20.
  • a stream 22 of pressurised LIN is fed to a reboiler/condenser 24 located outside the auxiliary column 14 where it is vaporised by indirect heat exchange against nitrogen-rich overhead vapour from the auxiliary column 14 to produce a stream 26 of pressurised GAN and nitrogen-rich liquid which is used as reflux for the auxiliary column 14.
  • a stream 28 of nitrogen-rich liquid is taken from the auxiliary column 14 and, after suitable pressure adjustment, fed as reflux to the ASU (not shown).
  • a stream 30 of oxygen-enriched bottoms liquid is taken from the auxiliary column 14 and also, after suitable pressure adjustment, fed as reflux to the ASU (not shown).
  • a stream 100 of feed air is compressed in compressor 102 and water and carbon dioxide are removed from the resultant stream of compressed feed air using purifying unit 104.
  • the purified compressed feed air is split into three streams 106, 108 and 122.
  • Stream 108 is cooled in the main heat exchanger 112 by indirect heat exchange against warming product streams to produce a stream 110 of cooled, compressed feed air which is then fed to the bottom of an HP column 124 of a dual distillation column system.
  • Stream 122 is further compressed in compressor 123 to produce a stream 126 of further compressed feed air which is then cooled in the main heat exchanger 112 to produce a stream 128 of cooled, further compressed feed air which is then fed, after suitable pressure adjustment, to an intermediate location on the HP column 124.
  • a second stream 325 of further compressed feed air is removed from an intermediate stage of the compressor 123 and cooled in the main heat exchanger 112 and then fed as stream 127 to the bottom of an auxiliary column 196.
  • Stream 106 of compressed feed air is further compressed in compressor 115 and the further compressed feed air is cooled in the main heat exchanger 112 to an intermediate temperature between the warm and cold ends thereof whereupon it is removed as stream 116 and expanded in expander 118 to provide refrigeration for the process.
  • the expanded stream 120 of feed air is fed to an intermediate location of the LP column 150 of the dual distillation column system.
  • the feed air fed as streams 110 and 128 to the HP column 124 is separated into HP column oxygen-rich bottoms liquid and HP column nitrogen-rich overhead vapour.
  • the feed air fed as stream 127 to the auxiliary column 196 is separated into auxiliary column oxygen-rich bottoms liquid and auxiliary column nitrogen-rich overhead vapour.
  • a stream 167 of auxiliary column oxygen-rich bottoms liquid is removed from the auxiliary column 196, reduced in pressure via valve 168 and combined with a stream of HP column oxygen-rich bottoms liquid from the HP column to form a stream 152 of oxygen-rich bottoms liquid which is fed, via valve 153, to an intermediate location of the LP column 150.
  • a stream 130 of liquid is removed from an intermediate location of the HP column 124 and fed, after pressure reduction via valve 131, to the LP column 150.
  • a stream 158 of HP column nitrogen-rich overhead vapour is removed from the top of the HP column 124 and condensed in condenser 160 located in the sump of the LP column 150 by indirect heat exchange against LOX to produce a stream 162 of LIN.
  • a portion of the LIN from stream 162 is fed as reflux to the top of the HP column 124.
  • a second portion is fed as stream 170, following pressure reduction across valve 171, as reflux to the top of the LP column 150.
  • a third portion is fed as stream 163 to a pump 164 where it is pumped to produce a stream 165 of pressurised LIN.
  • Stream 165 of pressurised LIN is boiled in reboiler/condenser 161 by indirect heat exchange against a stream 159 of auxiliary column nitrogen-rich overhead vapour to produce a stream 166 of pressurised GAN and a stream of nitrogen-rich liquid.
  • the pressurised GAN stream 166 is warmed in the main heat exchanger 112 against cooling feed air to produce a product stream 168 of pressurised GAN.
  • a portion of the nitrogen-rich liquid is fed as reflux to the top of the auxiliary column 196 and the remaining portion is fed as stream 169, after pressure reduction via valve 173, as reflux to the top of the LP column 150.
  • the feed streams to the LP column 150 are separated into LP nitrogen overhead vapour and LOX.
  • a stream 180 of LOX is removed from the LP column 150 and pressurised in pump 182 to produce a stream 184 of pressurised LOX which is warmed in the main heat exchanger 112 to produce a stream 186 of GOX.
  • a stream 172 of gaseous nitrogen is removed from the top of the LP column 150 and warmed in the main heat exchanger 112 to produce a stream 176 of LPGAN.
  • the auxiliary column 196 does not have a reboiler/condenser 161. Instead, the column has a further distillation zone 503 located above the main distillation zone 501.
  • Stream 165 of pressurised LIN is fed to the top of the auxiliary column 196 and stream 166 of pressurised GAN is removed from the top of the auxiliary column 196.
  • Stream 169 of nitrogen-rich liquid is removed from an intermediate location in the auxiliary column 196 and fed, after pressure reduction across valve 173, to the top of the LP column 150.
  • FIG. 5 The process depicted in Figure 5 is similar to that depicted in Figure 4 with the auxiliary column 196 having a further distillation section 503 located above the main distillation section 501.
  • An intermediate reflux stream to the HP column 124 is provided by a stream 169 of nitrogen-rich liquid which is reduced in pressure across valve 173.
  • Reflux for the LP column 150 is provided by stream 170 which is withdrawn from an intermediate location in the HP column, reduced in pressure across valve 171 and then fed to the top of the LP column 150.
  • FIG. 6 The process depicted in Figure 6 is similar to that depicted in Figure 3 with the auxiliary column 196 having a reboiler/condenser 161.
  • the main difference is in the air feed of the process.
  • the stream 100 of air is compressed in compressor 102 and the compressed stream purified in purifier 104 to remove the water and carbon dioxide.
  • a stream 105 of purified, compressed air is divided into three separate streams 107, 108 and 122.
  • Stream 108 of purified, compressed air is cooled in the main heat exchanger 112 and the cooled stream 110 is expanded in expander 118 to provide a portion of the refrigeration duty for the process.
  • the resultant expanded air stream is fed to the bottom of the HP column 124.
  • Stream 122 is further compressed in compressor 123 to produce a stream 126 of further compressed air which is cooled in the main heat exchanger 112.
  • the cooled, further compressed air is then fed, after pressure adjustment, as stream 128 to an intermediate location of the HP column 124.
  • Stream 107 is divided into two sub-streams.
  • the first sub-stream is cooled in the main heat exchanger 112 and then combined, after pressure adjustment, with the cooled, further compressed air from stream 126 and fed as stream 128 to the HP column 124.
  • the second sub-stream 325 is cooled in the main heat exchanger to form a stream 127 of cooled feed air which is fed to the bottom of the auxiliary column 196.
  • Stream 169 of nitrogen-rich liquid from the condenser 161 to the LP column 150, stream 165 of pumped LIN from the HP column 124 to the condenser 161, stream 170 of LIN from the HP column 124 to the LP column 150 and stream 130 of fluid from an intermediate location of the HP column 124 to the LP column 150 all pass through at least a portion of the main heat exchanger 112 in order that the temperature of each stream be adjusted to better match the temperatures of locations in the columns to which they are being fed.
  • the streams are not shown as passing through the main heat exchanger 112 but instead the exchanger 112 has been shown as split up.
EP05256250A 2004-10-12 2005-10-06 Procédé et dispositif pour la séparation cryogénique d'air Withdrawn EP1653183A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GBGB0422635.3A GB0422635D0 (en) 2004-10-12 2004-10-12 Process for the cryogenic distillation of air

Publications (1)

Publication Number Publication Date
EP1653183A1 true EP1653183A1 (fr) 2006-05-03

Family

ID=33443784

Family Applications (1)

Application Number Title Priority Date Filing Date
EP05256250A Withdrawn EP1653183A1 (fr) 2004-10-12 2005-10-06 Procédé et dispositif pour la séparation cryogénique d'air

Country Status (4)

Country Link
US (1) US20060075779A1 (fr)
EP (1) EP1653183A1 (fr)
CN (1) CN1760612A (fr)
GB (1) GB0422635D0 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008051259A2 (fr) * 2006-01-12 2008-05-02 Praxair Technology, Inc. Système de séparation cryogénique d'air
EP1878697A3 (fr) * 2006-07-14 2012-08-22 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Système et appareil pour la fourniture d'oxygène à basse pression et de faible pureté
WO2020169257A1 (fr) 2019-02-22 2020-08-27 Linde Gmbh Procédé et installation de décomposition d'air à basse température
EP3771873A1 (fr) * 2019-08-01 2021-02-03 Linde GmbH Procédé et installation de séparation d'air à basse température

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7712331B2 (en) * 2006-06-30 2010-05-11 Air Products And Chemicals, Inc. System to increase capacity of LNG-based liquefier in air separation process
EP2227624B1 (fr) * 2007-12-06 2020-04-29 Sustainable Energy Solutions, LLC Procédés et systèmes permettant de générer de l'énergie à partir d'une turbine utilisant de l'azote sous pression
KR101541742B1 (ko) * 2008-01-28 2015-08-04 린데 악티엔게젤샤프트 저온 공기 분리 방법 및 장치
DE102009048456A1 (de) * 2009-09-21 2011-03-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP2312247A1 (fr) * 2009-10-09 2011-04-20 Linde AG Procédé et dispositif de production d'azote liquide par décomposition de l'air à basse température
EP2770286B1 (fr) * 2013-02-21 2017-05-24 Linde Aktiengesellschaft Procédé et dispositif de collecte d'oxygène et d'azote sous haute pression
CN108168210A (zh) * 2018-01-25 2018-06-15 江西江氨科技有限公司 制氧方法及系统

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4433989A (en) 1982-09-13 1984-02-28 Erickson Donald C Air separation with medium pressure enrichment
US4790866A (en) 1986-11-24 1988-12-13 The Boc Group Plc Air separation
US5419137A (en) 1993-08-16 1995-05-30 The Boc Group, Inc. Air separation process and apparatus for the production of high purity nitrogen
US5596886A (en) 1996-04-05 1997-01-28 Praxair Technology, Inc. Cryogenic rectification system for producing gaseous oxygen and high purity nitrogen
EP0948730A1 (fr) * 1996-10-30 1999-10-13 Linde Aktiengesellschaft Procede et dispositif de production d'azote comprime
DE19933558A1 (de) * 1999-07-16 2000-09-28 Linde Tech Gase Gmbh Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
US6202442B1 (en) * 1999-04-05 2001-03-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'expoitation Des Procedes Georges Claude Integrated apparatus for generating power and/or oxygen enriched fluid and process for the operation thereof
US6276171B1 (en) 1999-04-05 2001-08-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Integrated apparatus for generating power and/or oxygen enriched fluid, process for the operation thereof
EP1271081A2 (fr) * 2001-06-12 2003-01-02 Air Products And Chemicals, Inc. Procédé de séparation de l'air
DE10339221A1 (de) * 2003-08-26 2005-03-24 Linde Ag Verfahren und Vorrichtung zur Erzeugung von Druckstickstoff durch Tieftemperaturzerlegung von Luft

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5098457A (en) * 1991-01-22 1992-03-24 Union Carbide Industrial Gases Technology Corporation Method and apparatus for producing elevated pressure nitrogen
GB9724787D0 (en) * 1997-11-24 1998-01-21 Boc Group Plc Production of nitrogen
FR2795496B1 (fr) * 1999-06-22 2001-08-03 Air Liquide Appareil et procede de separation d'air par distillation cryogenique
DE10139727A1 (de) * 2001-08-13 2003-02-27 Linde Ag Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4433989A (en) 1982-09-13 1984-02-28 Erickson Donald C Air separation with medium pressure enrichment
US4790866A (en) 1986-11-24 1988-12-13 The Boc Group Plc Air separation
US5419137A (en) 1993-08-16 1995-05-30 The Boc Group, Inc. Air separation process and apparatus for the production of high purity nitrogen
US5596886A (en) 1996-04-05 1997-01-28 Praxair Technology, Inc. Cryogenic rectification system for producing gaseous oxygen and high purity nitrogen
EP0948730A1 (fr) * 1996-10-30 1999-10-13 Linde Aktiengesellschaft Procede et dispositif de production d'azote comprime
US6202442B1 (en) * 1999-04-05 2001-03-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'expoitation Des Procedes Georges Claude Integrated apparatus for generating power and/or oxygen enriched fluid and process for the operation thereof
US6276171B1 (en) 1999-04-05 2001-08-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Integrated apparatus for generating power and/or oxygen enriched fluid, process for the operation thereof
DE19933558A1 (de) * 1999-07-16 2000-09-28 Linde Tech Gase Gmbh Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
EP1271081A2 (fr) * 2001-06-12 2003-01-02 Air Products And Chemicals, Inc. Procédé de séparation de l'air
DE10339221A1 (de) * 2003-08-26 2005-03-24 Linde Ag Verfahren und Vorrichtung zur Erzeugung von Druckstickstoff durch Tieftemperaturzerlegung von Luft

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
ANONYMOUS: "Nitrogen generation process", RESEARCH DISCLOSURE, MASON PUBLICATIONS, HAMPSHIRE, GB, vol. 464, no. 96, December 2002 (2002-12-01), XP007131872, ISSN: 0374-4353 *

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008051259A2 (fr) * 2006-01-12 2008-05-02 Praxair Technology, Inc. Système de séparation cryogénique d'air
WO2008051259A3 (fr) * 2006-01-12 2008-12-11 Praxair Technology Inc Système de séparation cryogénique d'air
EP1878697A3 (fr) * 2006-07-14 2012-08-22 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Système et appareil pour la fourniture d'oxygène à basse pression et de faible pureté
WO2020169257A1 (fr) 2019-02-22 2020-08-27 Linde Gmbh Procédé et installation de décomposition d'air à basse température
EP3771873A1 (fr) * 2019-08-01 2021-02-03 Linde GmbH Procédé et installation de séparation d'air à basse température

Also Published As

Publication number Publication date
CN1760612A (zh) 2006-04-19
GB0422635D0 (en) 2004-11-10
US20060075779A1 (en) 2006-04-13

Similar Documents

Publication Publication Date Title
EP1653183A1 (fr) Procédé et dispositif pour la séparation cryogénique d'air
EP0645595B1 (fr) Schémas de séparation d'air pour la coproduction d'oxygène et d'azote comme produit gazeux et/ou liquide
EP0697576B1 (fr) Procédé et dispositif de séparation d'air
JP2836781B2 (ja) 空気分離方法
US6314755B1 (en) Double column system for the low-temperature fractionation of air
EP0589646B1 (fr) Procédé de distillation pour la production d'azote dépourvu de monoxyde de carbone
EP0644388A1 (fr) Séparation cryogénique d'air
JP3169627B2 (ja) 空気分離方法
CA1283846C (fr) Procede de separation de l'air grace a la modification d'un generateur d'azote liquide a colonne de distillation unique
JPH07198249A (ja) 空気を分離するための方法および装置
EP1055890B1 (fr) Système de distillation cryogénique pour la séparation de l'air
US6202441B1 (en) Cryogenic distillation system for air separation
EP1470377A1 (fr) Procede integre et installation permettant la separation d'air alimente par de l'air comprime issu de plusieurs compresseurs
EP1055892B1 (fr) Système de distillation cryogénique pour la séparation de l'air
EP1055893B1 (fr) Système de distillation cryogénique pour la séparation des gaz de l'air
US5165244A (en) Process to produce oxygen and nitrogen at medium pressure
EP0831285A2 (fr) Séparation d'air
US20050210916A1 (en) Process and apparatus for the cryogenic separation of air
EP0831284B1 (fr) Séparation d'air
US11852408B2 (en) Method and apparatus for separating air by cryogenic distillation
EP1271080A1 (fr) Production d'azote à moyenne pression et à haut rendement d'extraction d'oxygène
EP1544560A1 (fr) Procédé et dispositif pour la production d'azote liquide

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 HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL BA HR MK YU

17P Request for examination filed

Effective date: 20060418

17Q First examination report despatched

Effective date: 20060707

AKX Designation fees paid

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

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: 20100501