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EP0793069A1 - Mit einem Aufkochkompressor versehener Generator für Sauerstoff von zwei Reinheitsgraden - Google Patents

Mit einem Aufkochkompressor versehener Generator für Sauerstoff von zwei Reinheitsgraden Download PDF

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Publication number
EP0793069A1
EP0793069A1 EP96301423A EP96301423A EP0793069A1 EP 0793069 A1 EP0793069 A1 EP 0793069A1 EP 96301423 A EP96301423 A EP 96301423A EP 96301423 A EP96301423 A EP 96301423A EP 0793069 A1 EP0793069 A1 EP 0793069A1
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EP
European Patent Office
Prior art keywords
column
stream
oxygen
purity
low
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Withdrawn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
EP96301423A
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English (en)
French (fr)
Inventor
Jeffrey Alan Hopkins
Jianguo Xu
Rakesh Agrawal
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
Priority to EP96301423A priority Critical patent/EP0793069A1/de
Priority to KR1019970005795A priority patent/KR970066477A/ko
Priority to ZA9701656A priority patent/ZA971656B/xx
Priority to IDP970571A priority patent/ID16093A/id
Priority to CN97110507A priority patent/CN1167246A/zh
Priority to JP9044150A priority patent/JPH102664A/ja
Publication of EP0793069A1 publication Critical patent/EP0793069A1/de
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—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
    • F25J3/04151—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
    • 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
    • F25J3/04248—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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04418—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system with thermally overlapping high and low pressure columns
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual 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
    • F25J2200/32—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • 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
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • 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
    • F25J2250/40—One fluid being air
    • 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 objective of the invention is to efficiently and cost-effectively generate two different oxygen purities from the same air separation plant, when only a small amount of high purity oxygen is required. It also provides a way to make small amounts of crude argon product if required on a plant which makes predominantly low purity oxygen. This is consistent with the requirements of new grass-roots steel mills based on the COREX steel-making process.
  • US-A-5,515,833 describes a cycle in which a portion of expanded gas from a compander is used to reboil the bottom reboiler of a dual-reboiler low pressure (“LP") column.
  • LP dual-reboiler low pressure
  • all air feed to the process is compressed to a pressure sufficient to allow the expander exhaust to reboil the high purity oxygen in the bottom reboiler of the LP column.
  • a high pressure nitrogen stream from the top of the high pressure (“HP”) column feeds an intermediate reboiler which is at a location above the low purity oxygen withdrawal location.
  • US-A-5,515,833 also shows an argon sidearm column connected to the main column between the two oxygen products withdrawal locations.
  • This feed location is necessary to eliminate nitrogen from the sidearm column feed.
  • it provides a sidearm column feed with a very low argon concentration (less than 4% Ar). This makes this distillation much more difficult than where the sidearm column feed is in the 9-14% Ar range. Due to low argon concentration in the feed to the sidearm column, for a given oxygen recovery, the argon recovery will be poor.
  • the present invention relates to cryogenic distillation of a stream containing nitrogen and oxygen to efficiently produce oxygen at at least two levels of purity.
  • the first product is a low-purity oxygen stream containing less than 97% oxygen (but generally greater than 80% oxygen) and the second product is a high purity oxygen product stream containing more than 97% oxygen, preferably more than 99.5% oxygen.
  • the high efficiency is achieved by taking a high efficiency process cycle for the production of low purity oxygen and modifying it according to the invention.
  • the high efficiency process cycle consists at least a distillation column where feed stream is distilled to produce low purity oxygen from the bottom and a nitrogen-rich stream from the top. The bottom of this column has a reboiler where a suitable process stream is condensed to provide boilup to the distillation column.
  • a liquid stream having an oxygen concentration at least equal to that of said feed stream is withdrawn either from the bottom of this first column (at the location of the bottom reboiler) or from a point which is some separation stages above the withdrawal location of the low purity oxygen and fed to the top of a sideleg column.
  • the bottom of the sideleg column is boiled by a suitable process fluid and high-purity oxygen product is withdrawn from the bottom of this sideleg column.
  • the vapour from top of the sideleg column is returned to the first column, preferably at same separation stage from where the liquid feed stream was withdrawn.
  • an argon sidearm column is attached at a proper location of the sideleg column producing high-purity oxygen, i.e., a vapour feed from an intermediate location of the sideleg column is fed to the argon sidearm column to produce argon from the top of this column and the liquid stream from the bottom of this column is returned back to the sideleg column.
  • a vapour feed from an intermediate location of the sideleg column is fed to the argon sidearm column to produce argon from the top of this column and the liquid stream from the bottom of this column is returned back to the sideleg column.
  • the present invention provides a process for cryogenic distillation of a compressed feed air stream in a distillation system comprising a low purity column producing a low purity (less than 97%) oxygen product stream and a nitrogen-rich stream, said column having a bottom reboiler in which a suitable first process stream is condensed to provide boilup to the column, characterized in that an oxygen-rich stream having an oxygen concentration at least equal to that of the feed to the low purity column is withdrawn from the distillation system and rectified in a high purity column whose bottoms reboiler heat is provided by condensation of a suitable second process stream to provide a high-purity (more than 97%) oxygen product stream, said second process stream being at a higher pressure than said first process stream.
  • the low purity oxygen product stream will contain more than 70% oxygen and preferably at least 90% oxygen.
  • the high purity oxygen product stream preferably contains at least 99.5% oxygen.
  • the distillation system comprises a high pressure column and a low pressure column and:
  • the process stream providing bottom reboil to the high purity column is a portion of the compressed feed air which has been further compressed. At least a portion of this compressed feed air portion can be is fed to the high pressure column and/or to the low pressure column.
  • the process stream providing bottom reboil to the high purity column can be at least a portion of the high pressure nitrogen overhead which has been further compressed.
  • the oxygen-rich stream can be withdrawn from the low pressure column, usually the sump thereof, and, preferably, the oxygen-lean overhead vapour is returned to the low pressure column at substantially the same location as that at which the oxygen-rich stream was withdrawn.
  • the oxygen-rich stream can be withdrawn from the high pressure column, suitably as a portion of the high pressure crude liquid oxygen bottoms.
  • a vapour stream can be withdrawn from the low pressure column at a location below the feed of the high pressure crude liquid oxygen bottoms thereto and fed to the high purity column at a location below the feed of the oxygen-rich stream thereto.
  • the process stream providing bottom reboil to the low pressure column can be at least a portion of the high pressure nitrogen overhead or a portion of the compressed feed air. When it is a portion of the compressed air feed, at least a portion of the resultant condensed fed can be fed to the high pressure column and/or to the low pressure column. If the high pressure nitrogen overhead is not condensed to provide low pressure column reboil, at least a portion thereof can be condensed at an intermediate location in the low pressure column.
  • an argon rich vapour stream withdrawn from an intermediate location of the high purity column can be separated in an argon column to produce an argon product stream and a liquid argon-depleted stream which is returned to the high purity column.
  • the oxygen-rich stream suitably is withdrawn from the low pressure column at a location above said intermediate location and an argon rich vapour stream withdrawn from an intermediate location of the high purity column is separated in an argon column to produce an argon product stream and a liquid argon-depleted stream which is returned to the high purity column.
  • Argon overhead from an argon column can be condensed by boiling a portion of the high pressure crude liquid oxygen bottoms and the vaporized high pressure crude liquid oxygen bottoms fed to the low pressure column and/or to the high purity column.
  • a portion of the compressed air feed can be fed to the low pressure column or a portion of the compressed air feed further compressed to a higher pressure than the main compressed air feed portion to the high pressure column and at least a portion of the further compressed feed air portion fed to the high pressure column and/or to the low pressure column.
  • At least a portion of the condensed high pressure nitrogen overhead can be fed to the low pressure column as reflux.
  • all of the condensed high pressure nitrogen overhead can be fed to the high pressure column as reflux and the low pressure column refluxed with a sidestream withdrawn from the high pressure column.
  • a portion of the nitrogen rich sidestream can be fed to the high purity column.
  • the low purity oxygen product stream can be boiled against the portion of the compressed air feed fed to the high pressure column to at least partially vaporize the compressed air feed portion.
  • the low purity oxygen product stream and high purity oxygen product stream can be withdrawn from the low pressure column and high purity column respectively as liquids and pumped prior to heat exchange with the main compressed air feed to generate pressurized oxygen products.
  • the present invention also provides an apparatus for producing low purity oxygen and high purity oxygen products by the cryogenic distillation of a compressed air feed by the process of Claim 1, said apparatus comprising:
  • a system comprising a HP column (15), a LP column (25) and a sideleg column (23) is used.
  • Low purity oxygen product (95% GOX) is obtained from the bottom of the LP column (25).
  • High purity oxygen product (99.5% GOX) is obtained from the bottom of the sideleg column (23), in which a liquid stream (35) from the bottom of the LP column (25) is distilled and boiled by a portion (21) of the feed air (10) which has been boosted in pressure.
  • Vapour (37) from the top of the sideleg column (23) is returned to the bottom of the LP column (25).
  • clean, dry compressed air (10) from a front-end purification system (1) is split into three streams (11, 12, 13).
  • a first feed air stream (11) is fed directly to a main heat exchanger (14), where it is cooled to near its dew point temperature, and then (11') to the HP column (15).
  • a second feed air stream (12) is fed via the compressor end (16) of a compander (17) to the main heat exchanger (14) from which it is withdrawn as a side stream (18) and fed via the expander end (19) of the compander (17) to the LP column (25).
  • the compander (17) generates refrigeration for the cycle.
  • a third feed air stream (13) is fed via a low pressure booster air compressor (20) to the main heat exchanger (14) where it is cooled to near its dew point.
  • the resultant cooled stream (21) is fed to a reboiler (22) in the bottom of the high purity or sideleg column (23) to provide reboil to that column.
  • the liquified air (24) from this reboiler (22) is fed to the HP column (15).
  • some or all of the liquified air (24) can be subcooled and fed to the LP column (25) rather than to the HP column (15).
  • the HP column (15) provides an initial distillation of air to generate a liquid oxygen-enriched (crude LOX) stream (26) at the bottom of the column and a HP gaseous nitrogen stream (27) at the top of the column.
  • the crude LOX stream (26) has an oxygen content usually greater than 30% and more often greater than 35%.
  • This stream (26) is subcooled against a LP gaseous nitrogen stream (28) from the top of the LP column (25) in a subcooler (29) and is then reduced in pressure and fed to an intermediate location of the LP column (25).
  • the warmed LP gaseous nitrogen stream (28') is further warmed in the main heat exchanger (14) before being vented to atmosphere (WASTE) or recovered as a coproduct stream.
  • At least the majority (30) of the HP gaseous nitrogen (27) from the top of the HP column (15) is fed to a reboiler (31) in the bottom of the LP column (25).
  • the condensed nitrogen stream from this reboiler (31) is split to provide two substreams (32, 33).
  • One substream (32) is used to reflux the HP column (15) and the other substream (33) is cooled in the subcooler (29) and then used to reflux the LP column (25).
  • Part (34) of the gaseous nitrogen stream (27) withdrawn from the top of the HP column (15) is warmed in the main heat exchanger (14) for recovery as product (GAN). If no product nitrogen is required, all of the withdrawn HP nitrogen stream (27) can be fed to the reboiler (31). However, if large amounts of product nitrogen are required, it is typically more efficient to take this from the LP column (25).
  • a low purity liquid oxygen stream (35) is withdrawn from the sump of the LP column (25) and fed to the top of the sideleg column (23).
  • the low purity liquid oxygen is distilled and boiled against the cooled third feed air stream (21) fed to the reboiler (22).
  • a high purity gaseous oxygen stream (36) is removed from above the sump of the sideleg column (23) and fed to the main heat exchanger (14) from where it is recovered as product (99.5% GOX).
  • An oxygen-lean overhead vapour stream (37) is returned from the sideleg column (23) to the LP column (25) just above the sump thereof.
  • liquid feed (35) for the sideleg column (23) is withdrawn from a location of the LP column (25) which is below the crude LOX feed (26'), the concentration of oxygen in the liquid feed (35) is greater than that in the crude LOX feed (26').
  • a low purity oxygen product stream (38) is withdrawn from the bottom of the LP column (25) and fed to the main heat exchanger (14) from where it is recovered as product (95% GOX).
  • a separate booster (20) is provided to compress the third feed air stream (13) used to provide reboil in heat exchanger (22) to the bottom of the sideleg column (23).
  • this feed air stream (13) could be boosted in the compressor end (16) of the compander system (17).
  • the embodiment of Figure 2 differs from that of Figure 1 in that the low purity oxygen stream (38) is withdrawn from the LP column (25) as a liquid stream and is boiled against a portion (215) of the first cooled feed air stream (11) in a LOX boil vaporizer (210); the reboiler (31) is relocated to an intermediate location in the LP column (25); and a further reboiler (211) fed by a cooled feed air stream (212) is located in the bottom of the LP column (25). Only the differences in the two systems will be described.
  • a minor portion of the cooled first feed air stream (11') is withdrawn as a substream (212) and is fed to the bottom reboiler (211) in the LP column (25).
  • the condensed air (213) from this reboiler (211) is fed to an intermediate location of the HP column (15).
  • the remaining (larger) portion (215) of the cooled first feed air stream (11') is partially condensed in the LOX boil vaporizer (210) by heat exchange with the low purity liquid oxygen product (38) from the LP column (25).
  • the resultant two-phase feed air stream (214) is then fed to the bottom of the HP column (15).
  • the condensed air (213) can be fed to the HP column (15) at the same place as the two-phase air feed (214) instead of to the intermediate location. This arrangement is simpler but less efficient than feed to the midpoint.
  • Some or all of the liquified air from the air-fed reboilers (22, 211) can be cooled in subcooler (29) and fed to the LP column (25) instead of to the HP column (15).
  • At least the major portion of the HP gaseous nitrogen stream (27) from the top of the HP column is fed to the reboiler (31) which, relative to the system of Figure 1, has been relocated at an intermediate location in the LP column (25).
  • the oxygen stream (38) is boiled by the cooled first air stream (215) and then warmed in the main heat exchanger (14) for recovery as product (95% GOX).
  • the LOX boil vaporizer (210) increases the pressure of the low purity oxygen vapour thus reducing compression power.
  • the embodiment of Figure 3 differs from that of Figure 2 in that the second feed air stream (12) is boosted in pressure by a compressor (310); the exhaust (311) from the expander end (19) of compander (17) is fed to the HP column (15) instead of to the LP column (25); additional air feed (312/313, 312/314) is provided to the LP column (25) and/or to the HP column (15); the non-reflux portion (33) of the condensed HP nitrogen stream (315) is withdrawn as eventually gaseous product (GAN) instead of being fed to the LP column (25); the LOX boil vaporizer is omitted; the high purity oxygen product (36) stream is withdrawn from the sideleg column (23) as liquid; the low purity oxygen stream (38), high purity oxygen stream (36) and nitrogen product stream (33) are pumped using liquid pumps (316, 317, 318) to generate pressurized oxygen and nitrogen products; and the LP column (25) is refluxed with a side stream (319) from the HP column (15). Only the differences in the two systems will
  • a portion (215) of the cooled first feed air stream (11') remaining after withdrawal of the substream (212) is fed directly to the bottom of the HP column (15).
  • the second feed air stream (12) is compressed in a high pressure booster air compressor (310) and split into two substreams (312, 320).
  • the larger of the substreams (312), containing the majority of the compressed air, is fed to the main heat exchanger (14) where it is condensed to vaporize the liquid products.
  • part of the liquified air (314) can be fed to the HP column (15) and the remainder (313) cooled in the subcooler (29) and fed to the LP column (25).
  • all of the liquified air could be fed to the HP column (15) or to the LP column (25).
  • the smaller substream (320) of the air from the booster compressor (310) is fed to the compressor end (16) of the compander (17) and, after partial cooling in the main heat exchanger (14) is fed to the expander end (19) of the compander (17) to generate refrigeration for the plant.
  • the expander exhaust (311) is combined with the cooled first feed air stream portion (215) fed to the bottom of the HP column (15).
  • the compander feed can be taken as a sidestream from an inter-stage of the booster compressor (310) instead of from the booster compressor discharge as shown in Figure 3.
  • the compander (17) is omitted and the partially cooled substream (320) is fed from the main heat exchanger (14) to an expander replacing the expander end (19) of the compander (17).
  • the compressed third feed air stream (13) required to reboil the sideleg column (23) can be withdrawn as a sidestream from the common booster compressor or from the common booster compressor discharge product.
  • a side stream (319) of impure reflux is withdrawn from the HP column (15) several stages below the top, cooled in the subcooler (29) and fed (319') to the top of the LP column (25).
  • the HP nitrogen stream (27) withdrawn from the top of the HP column (15) is condensed in the intermediate reboiler (31) and the condensed HP nitrogen stream divided into a reflux substream (32) and a product stream (33).
  • the product stream (33) is pumped by a liquid pump (318) prior to vaporization in the main heat exchanger (14) for collection as gaseous nitrogen product (GAN).
  • the low purity liquid oxygen stream (38) withdrawn from the sump of the LP column (25) also is pumped by a liquid pump (316) prior to vaporization in the main heat exchanger (14) for collection as low purity gaseous oxygen product (95% GOX).
  • the high purity liquid oxygen stream (36) from the sideleg column (23) is pumped by liquid pump (317) prior to vaporization in the main heat exchanger (14) for collection as high purity gaseous oxygen product (99.5% GOX)
  • the embodiment of Figure 4 is a simplification of that of Figure 2 in which the LOX boil vaporizer (210) is omitted and the (larger) portion (215) of the cooled first feed air stream (11') is fed directly to the bottom of the HP column (15).
  • the low purity oxygen product stream (438) is withdrawn from the sump of the LP column (25) as gas instead of as liquid.
  • Figure 5 differs from that of Figure 2 in that the feed to and return from the sideleg column (23) is at a location of the LP column (25) above the intermediate reboiler (31) and an argon sidearm column (510) has been added. Only the differences in the two systems will be described.
  • the feed stream (35) to the sideleg column (23), instead of being withdrawn from the sump of the LP column (25) as in Figure 2, is withdrawn from the middle of that column, above the intermediate reboiler (31).
  • the feed stream (35) to the sideleg column (23) could be withdrawn at a location below the intermediate reboiler (31) but above the sump of the LP column (25).
  • the vapour stream (37) from the top of the sideleg column (23) is returned preferably to this same point in the LP column (25).
  • High purity oxygen product stream (36) is withdrawn from the bottom of the column (23) either as gas (as in Figure 2) or as liquid (as in Figure 3).
  • An argon rich vapour sidestream (511) is withdrawn from the middle of the sideleg column (23) at a point where there is low nitrogen content in the column vapour.
  • the nitrogen concentration in the argon rich vapor sidestream (511) usually is less than 1%, preferably less than 0.5% and especially less than 100 ppm.
  • the argon rich sidestream (511) is distilled further in a crude argon or sidearm column (510).
  • the product from this column is mostly argon and can contain as much a 4% or as little as 1 ppm of oxygen, depending on the number of stages in the column.
  • the sidestream (511) can be further purified if necessary with any suitable purifier.
  • An argon depleted liquid stream (512) from the bottom of the sidearm column (510) is returned to the middle of the sideleg column (23) preferably at the same point where the vapour sidestream (511) was withdrawn.
  • the argon at the top of the sidearm column (510) is condensed by boiling a portion (513) of the subcooled crude LOX in a reboiler (514).
  • the vaporized crude LOX (crude GOX, 515) is fed to a suitable point in the LP column (25).
  • a portion of the argon stream from the top of the sidearm column (510) is recovered as an argon product stream.
  • said argon product stream is a portion (520) of the condensed stream from the reboiler (514).
  • Figure 6 differs from that of Figure 3 in that the sideleg column (23) is decoupled from the LP column (25) and an argon sidearm column (510) has been added. Only the differences in the two systems will be described.
  • the feed to the sideleg column instead of being withdrawn from the LP column (25), is provided by feeding to the top of the sideleg column (23) a portion (610) of the subcooled nitrogen rich impure reflux (319) and feeding to an intermediate location of the sideleg column (23) a subcooled portion (611) of the crude LOX reflux (26) to the LP column (25).
  • the vapour stream (612) from the top of sideleg column (23) is oxygen depleted waste and is mixed with the oxygen depleted waste (28) from the top of the LP column (25).
  • High purity oxygen product (36) is withdrawn from the bottom of the sideleg column (23) either as liquid (as in Figure 3) or as gas (as in Figure 2).
  • An argon rich vapour sidestream (511) is withdrawn from the middle of the sideleg column (23) at a point where there is low nitrogen content in the column vapor.
  • the nitrogen concentration in the argon rich vapor sidestream (511) usually is less than 1%, preferably less than 0.5% and especially less than 100 ppm.
  • the argon rich sidestream (511) is distilled further in the sidearm column (510).
  • the product from this column is mostly argon and can contain as much a 4% or as little as 1 ppm of oxygen, depending on the number of stages in the column.
  • the sidestream (511) can be further purified if necessary with any suitable purifier.
  • An argon depleted liquid stream (512) from the bottom of the sidearm column (510) is returned to the middle of the sideleg column (23) preferably at the same point where the vapour sidestream (511) was withdrawn.
  • the argon at the top of the sidearm column (510) is condensed by boiling a portion (513) of the subcooled crude LOX in a reboiler (514).
  • the vaporized crude LOX (crude GOX, 613) is fed to a suitable point in the sideleg column (23).
  • a portion (520) of the condensed argon stream from the reboiler (514) is recovered as an argon product stream.
  • a vapour stream can be withdrawn from a stage below the crude LOX feed (26) to the LP column (25) and fed to the sideleg column (23) at a location which is below the feed point of the vaporized crude LOX (613).
  • Figure 7 differs from that of Figure 6 in that the vaporized crude LOX (713) from the top of the sidearm column (510) is fed to the LP column (25) and a vapour stream (711) withdrawn from the LP column (25) from a location below this feed is fed to the sideleg column (23).
  • the nitrogen product stream (GAN) is compressed in the LP booster compressor (20) instead of the third feed air stream (13).
  • the compressed nitrogen product stream is fed to the reboiler (22) in the sideleg column (23).
  • the resultant condensed nitrogen can be fed to any suitable point of the HP column (15).
  • the pressure of the supply air from the front end (1) is only as high as it needs to be to boil low purity oxygen. This is consistent with the low pressure of a dual-reboiler cycle. Only the portion of the air necessary to make the sideleg oxygen is compressed to the pressure required to boil high purity oxygen. This reduces the compression power over cycles where the entire air feed is used to make high purity oxygen and compared with the cycle of US-A-5,515,833.
  • the new cycle of the invention also permits of reduction in size of the LP column (25). If the sideleg column (23) is decoupled as in Figure 6, the overall diameter of the LP column (25) is smaller because it is not purifying the entire air stream. It also permits of reduction in the number of stages which must be of a large diameter, since the large main column (15, 25) no longer has to make high purity oxygen.
  • this feed is rich in argon (typically 6-22%, preferably 9-15%, Ar). This not only simplifies and shortens the sidearm column over the cycle of US-A-5,515,833 which must start with a feed severely depleted in argon (typically less than 4% Ar), but provides much higher recoveries of argon.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP96301423A 1996-03-01 1996-03-01 Mit einem Aufkochkompressor versehener Generator für Sauerstoff von zwei Reinheitsgraden Withdrawn EP0793069A1 (de)

Priority Applications (6)

Application Number Priority Date Filing Date Title
EP96301423A EP0793069A1 (de) 1996-03-01 1996-03-01 Mit einem Aufkochkompressor versehener Generator für Sauerstoff von zwei Reinheitsgraden
KR1019970005795A KR970066477A (ko) 1996-03-01 1997-02-25 재비등기 압축기를 구비한 이중 순도의 산소 발생기
ZA9701656A ZA971656B (en) 1996-03-01 1997-02-26 Dual purity oxygen generator with reboiler compressor.
IDP970571A ID16093A (id) 1996-03-01 1997-02-26 Generator oksigen kemurnian ganda dan kompresor pendidih ulang
CN97110507A CN1167246A (zh) 1996-03-01 1997-02-26 带有再沸器压缩机的双纯氧发生器
JP9044150A JPH102664A (ja) 1996-03-01 1997-02-27 低純度及び高純度の酸素製品を製造する圧縮原料空気流の低温蒸留方法

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EP96301423A EP0793069A1 (de) 1996-03-01 1996-03-01 Mit einem Aufkochkompressor versehener Generator für Sauerstoff von zwei Reinheitsgraden

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ZA (1) ZA971656B (de)

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EP0823604A2 (de) * 1996-08-05 1998-02-11 Praxair Technology, Inc. Kryogenisches Rektifikationssystem zur Herstellung von niedrigreinem Sauerstoff und hochreinem Sauerstoff
US5865041A (en) * 1998-05-01 1999-02-02 Air Products And Chemicals, Inc. Distillation process using a mixing column to produce at least two oxygen-rich gaseous streams having different oxygen purities
EP0962732A1 (de) * 1998-06-02 1999-12-08 Air Products And Chemicals, Inc. Stickstoffgenerator mit mehreren Säulen und gleichzeitiger Sauerstofferzeugung
FR2787561A1 (fr) * 1998-12-22 2000-06-23 Air Liquide Procede de separation d'air par distillation cryogenique
FR2787559A1 (fr) * 1998-12-22 2000-06-23 Air Liquide Procede et installation de separation d'air par distillation cryogenique
EP1146302A2 (de) * 2000-04-14 2001-10-17 Praxair Technology, Inc. Kryogenisches Luftzerlegungsystem mit integrierter Wärme- und Stoffübertragung
FR2930330A1 (fr) * 2008-04-22 2009-10-23 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
FR2943772A1 (fr) * 2009-03-27 2010-10-01 Air Liquide Appareil et procede de separation d'air par distillation cryogenique
WO2012136939A2 (fr) 2011-04-08 2012-10-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d'air par distillation cryogenique
WO2014102014A3 (de) * 2012-12-27 2015-05-28 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperatur-luftzerlegung
CN104833174A (zh) * 2015-05-26 2015-08-12 杭州杭氧股份有限公司 一种带压辅助氧塔低能耗生产带压低纯氧和高纯氧产品的装置及方法
CN113670003A (zh) * 2021-07-29 2021-11-19 北京科技大学 高安全性的储能、发电和物质回收外压缩空分工艺流程

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FR2898134B1 (fr) * 2006-03-03 2008-04-11 Air Liquide Procede d'integration d'un haut-fourneau et d'une unite de separation de gaz de l'air
US8191386B2 (en) * 2008-02-14 2012-06-05 Praxair Technology, Inc. Distillation method and apparatus
FR2953915B1 (fr) * 2009-12-11 2011-12-02 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
WO2012004242A2 (fr) * 2010-07-05 2012-01-12 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil et procede de separation d'air par distillation cryogenique
CN102080921B (zh) * 2010-12-23 2013-09-04 上海启元科技发展有限公司 一种高压氮和低压氧的生产方法及装置
CN102445054A (zh) * 2011-12-22 2012-05-09 开封黄河空分集团有限公司 一种由空气分离制取氧气和氮气的工艺
PL2770286T3 (pl) * 2013-02-21 2017-10-31 Linde Ag Sposób i urządzenie do pozyskiwania tlenu pod wysokim ciśnieniem i azotu pod wysokim ciśnieniem
FR3010778B1 (fr) * 2013-09-17 2019-05-24 Air Liquide Procede et appareil de production d'oxygene gazeux par distillation cryogenique de l'air
JP6159242B2 (ja) * 2013-12-13 2017-07-05 大陽日酸株式会社 空気分離方法及び装置
CN105066587A (zh) * 2015-09-16 2015-11-18 开封空分集团有限公司 深冷分离及生产低纯度氧、高纯度氧和氮的装置及方法
CN109737691B (zh) * 2019-01-31 2020-05-19 东北大学 一种钢铁企业空气分离系统

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EP0823604A3 (de) * 1996-08-05 1998-09-09 Praxair Technology, Inc. Kryogenisches Rektifikationssystem zur Herstellung von niedrigreinem Sauerstoff und hochreinem Sauerstoff
EP0823604A2 (de) * 1996-08-05 1998-02-11 Praxair Technology, Inc. Kryogenisches Rektifikationssystem zur Herstellung von niedrigreinem Sauerstoff und hochreinem Sauerstoff
US5865041A (en) * 1998-05-01 1999-02-02 Air Products And Chemicals, Inc. Distillation process using a mixing column to produce at least two oxygen-rich gaseous streams having different oxygen purities
EP0962732A1 (de) * 1998-06-02 1999-12-08 Air Products And Chemicals, Inc. Stickstoffgenerator mit mehreren Säulen und gleichzeitiger Sauerstofferzeugung
FR2787561A1 (fr) * 1998-12-22 2000-06-23 Air Liquide Procede de separation d'air par distillation cryogenique
FR2787559A1 (fr) * 1998-12-22 2000-06-23 Air Liquide Procede et installation de separation d'air par distillation cryogenique
EP1146302A2 (de) * 2000-04-14 2001-10-17 Praxair Technology, Inc. Kryogenisches Luftzerlegungsystem mit integrierter Wärme- und Stoffübertragung
EP1146302A3 (de) * 2000-04-14 2003-01-08 Praxair Technology, Inc. Kryogenisches Luftzerlegungsystem mit integrierter Wärme- und Stoffübertragung
WO2009136075A3 (fr) * 2008-04-22 2010-10-07 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procede et appareil de production d ' oxygene par separation d ' air par distillation cryogenique
FR2930330A1 (fr) * 2008-04-22 2009-10-23 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
WO2009136075A2 (fr) * 2008-04-22 2009-11-12 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procede et appareil de separation d'air par distillation cryogenique
FR2943772A1 (fr) * 2009-03-27 2010-10-01 Air Liquide Appareil et procede de separation d'air par distillation cryogenique
WO2010109149A3 (fr) * 2009-03-27 2011-09-15 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil et procédé de séparation d'air par distillation cryogénique
WO2012136939A2 (fr) 2011-04-08 2012-10-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d'air par distillation cryogenique
FR2973865A1 (fr) * 2011-04-08 2012-10-12 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
WO2012136939A3 (fr) * 2011-04-08 2015-01-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d'air par distillation cryogenique
US9696087B2 (en) 2011-04-08 2017-07-04 L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude Method and apparatus for separating air by cryogenic distillation
WO2014102014A3 (de) * 2012-12-27 2015-05-28 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperatur-luftzerlegung
CN104833174A (zh) * 2015-05-26 2015-08-12 杭州杭氧股份有限公司 一种带压辅助氧塔低能耗生产带压低纯氧和高纯氧产品的装置及方法
CN113670003A (zh) * 2021-07-29 2021-11-19 北京科技大学 高安全性的储能、发电和物质回收外压缩空分工艺流程
CN113670003B (zh) * 2021-07-29 2022-08-09 北京科技大学 高安全性的储能、发电和物质回收外压缩空分工艺流程

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CN1167246A (zh) 1997-12-10

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