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EP0093448A2 - Process and apparatus for obtaining gaseous oxygen at elevated pressure - Google Patents

Process and apparatus for obtaining gaseous oxygen at elevated pressure Download PDF

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Publication number
EP0093448A2
EP0093448A2 EP83104318A EP83104318A EP0093448A2 EP 0093448 A2 EP0093448 A2 EP 0093448A2 EP 83104318 A EP83104318 A EP 83104318A EP 83104318 A EP83104318 A EP 83104318A EP 0093448 A2 EP0093448 A2 EP 0093448A2
Authority
EP
European Patent Office
Prior art keywords
heat exchange
exchange device
compressed
gas stream
pressure
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP83104318A
Other languages
German (de)
French (fr)
Other versions
EP0093448A3 (en
EP0093448B1 (en
Inventor
Werner Dipl.-Ing. Skolaude
Gunnar Dr. Rer.Nar. Eggendorfer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE19823216502 external-priority patent/DE3216502A1/en
Priority claimed from DE19823216510 external-priority patent/DE3216510A1/en
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to AT83104318T priority Critical patent/ATE22991T1/en
Publication of EP0093448A2 publication Critical patent/EP0093448A2/en
Publication of EP0093448A3 publication Critical patent/EP0093448A3/en
Application granted granted Critical
Publication of EP0093448B1 publication Critical patent/EP0093448B1/en
Expired 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
    • F25J3/04151—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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure 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
    • F25J3/04006—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
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
    • F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air
    • Y10S62/94—High pressure column

Definitions

  • the invention relates to a process for the production of gaseous oxygen under elevated pressure by low-temperature rectification of air, in which air is compressed, cleaned and at least partially cooled in a first heat exchange device in heat exchange with decomposition product and passed into the rectification, while a second gas stream is passed onto one compressed higher pressure and cooled in a second heat exchange device in heat exchange with decomposition product, relaxed and also passed into the rectification, and in which oxygen is removed from the rectification in liquid form, pumped to the desired pressure, in heat exchange with the gas stream compressed to higher pressure is evaporated and heated, and a device for performing the method.
  • the invention has for its object to develop a method of the type mentioned, in which the energy consumption in oxygen production is reduced.
  • This object is achieved in that a third partial stream of the gas to be decomposed is cooled in heat exchange with the decomposition product.
  • a part of the compressed, purified air is cooled in the first heat exchange device as a third gas stream, at least partially removed from it at an intermediate point and expanded to perform work, and heat is transferred from an intermediate point of the second heat exchange device to an intermediate point of the first heat exchange device .
  • the temperature difference at the cold end is reduced by the removal of heat at an intermediate point of the second heat exchange device.
  • the amount of heat removed is fed to the first heat exchange device, so that less air is required for heating in the cold part.
  • This part of the air which has been cut in is removed from the first heat exchange device before it has cooled down.
  • This partial air flow referred to as the third gas flow, is expanded while performing work, with cooling being generated.
  • the inlet temperature during expansion is determined by the narrowest temperature difference in the second heat exchange device.
  • the provision of additional heat according to the invention in the first heat exchange device can result in a larger amount of gas in favor of a smaller amount of gas in the are passed through the second heat exchange device so that the amount of the second gas flow in the second heat exchange device, which is compressed to a relatively high pressure, can also be reduced.
  • the energy losses at the warm end of the second heat exchange device are reduced by reducing the volume flows.
  • the third gas stream is further compressed before it cools down.
  • the further compression brings greater pressure slope and thus the same cooling capacity with a smaller amount of gas, so that the main compressor for the incoming air can be reduced.
  • a lower final temperature is reached during the expansion, so that the yield of the rectification is improved.
  • the third gas stream is expediently introduced into the rectification and / or into the nitrogen withdrawn from the rectification after it has expanded.
  • the third gas stream is withdrawn from the first heat exchange device essentially at the point at which the heat is supplied.
  • the relaxation during work offers the advantage that less air has to be compressed on the main air compressor.
  • the additional generation of cold associated with the work-performing relaxation can be used to make the temperature difference at the warm and thus at the cold end of the first and / or second heat exchange device larger, so that the amount of the second gas flow can be reduced.
  • a portion of the compressed second gas stream is cooled in heat exchange with a portion of a gas stream to be heated in the first heat exchange device from the rectification before the end of its cooling.
  • the heat-releasing second partial flow is either fed to the remaining part of the second gas flow, preferably after leaving the second heat exchange device, or fed separately from the latter to the rectification.
  • the heat-absorbing gas stream is conducted at an intermediate point into the first heat exchange device and heated either together with the remaining gas stream from which it was taken or separately from it.
  • the compression of the second gas stream is carried out in two stages, a partial stream being branched off between the two stages, cooled in the second heat exchange device and relaxed before the end of the heat exchange and carried out for rectification.
  • the splitting of the second gas stream has the advantage that the inlet pressures on the expansion machines can be optimized in each case when the two partial streams of the second gas stream are depressurized.
  • a portion of the second gas stream compressed to its final pressure is branched off before the end of the heat exchange, expanded to perform work and fed to the rectification.
  • the branched partial stream is expanded at a higher inlet temperature than the rest of the second gas stream removed at the cold end of the second heat exchange device. This increases the cooling capacity, moreover. the wet steam area is avoided during relaxation. As an additional advantage, small temperature differences occur at the cold end of the second heat exchange device.
  • the second gas flow is a partial flow of the air to be separated or a gas flow from the pressure stage.
  • the second gas flow is branched off in front of the first heat exchange device.
  • a gas stream is taken from the pressure stage, the nitrogen content of which is equal to or greater than that of air, heated in one of the two or in parallel in both heat exchange devices and then compressed.
  • part of the second gas flow is used as the third partial flow, the second gas flow being split into two partial flows, which are cooled separately from one another at different pressures in the second heat exchange device, and in that the partial flow with the lower pressure a higher temperature than the partial flow with the higher pressure is removed from the heat exchange device, relaxed during work and passed into the rectification.
  • the high-pressure gas stream which is used to evaporate the oxygen is divided into two sub-streams of different pressure, which are passed separately through the heat exchange device.
  • This measure allows the quantities and pressures of the two partial flows to be varied without a significant change in the compression energy.
  • the pressure and quantity of the partial flow with the lower pressure can be selected so that its work-relieving expansion takes place under optimal conditions, depending on the inlet temperature into the expansion machine determined by the oxygen delivery pressure, i.e. in a pressure range in which the performance maximum lies.
  • the pressure of the higher compressed partial flow can be varied within wide limits, which means that the oxygen delivery pressure can also be varied within wide limits.
  • the partial flow at a higher pressure is relieved of work after its cooling.
  • the compression energy is used optimally.
  • the high cooling capacity due to the separate expansion of the two partial flows enables relatively large temperature differences at the warm ends of the heat exchange devices, as a result of which the necessary amount of compressed air can be kept low.
  • there is no compression of additional air for cooling i.e. the total amount of air becomes a minimum depending on the desired decomposition products.
  • the main air compressor and cleaning stage are dimensioned as small as possible.
  • the pressure of the partial flow with the lower pressure is. according to an embodiment of the method according to the invention. between 10 bar and 60 bar.
  • the preferred pressure range is between 20 and 40 bar.
  • the respective pressure depends on the pressure of the oxygen.
  • the partial flow with the lower pressure in the region of the lowest temperature difference between the partial flow with the higher pressure and the oxygen is removed from the second heat exchange device.
  • the temperature difference at the end of the second heat exchange device is relatively large and assumes a minimum at an intermediate point of the heat exchange device. This is the preferred point of withdrawal for the lower compressed partial flow.
  • the temperature difference at the cold end of the heat exchange device is reduced, and thus the energy requirement of the Procedure.
  • the work performed in relieving the pressure on one of the two and / or both partial flows is used for post-compression of the one or both partial flows. Coupling one or both expansion machines with one or both post-compressors reduces energy consumption.
  • heat is transferred from an intermediate point of one to an intermediate point of the other heat exchange device.
  • the heat exchange takes place either indirectly or by direct transfer of a gas flow from one to the other heat exchange device. This measure proves to be very effective in order to optimize the temperature differences at the heat exchange devices.
  • a portion of the compressed, purified air be branched off at an intermediate point of the first heat exchange device, relaxed in order to perform work, and passed into the rectification. This increases the cooling capacity if the cooling capacity from the expansion of the medium and high pressure flow is insufficient.
  • the second gas stream is preferably a partial stream of the incoming air.
  • the second gas flow from the pressure removed stage and warmed and compressed before its splitting.
  • This gas stream is either a gas stream from the lower region of the pressure stage with a composition such as air, or a nitrogen-rich gas stream from the upper region of the pressure stage.
  • a part of the second gas stream is post-compressed before it is compressed, cooled in one of the heat exchange devices, removed from it at an intermediate point, expanded in a work-performing manner and passed into the rectification.
  • a device for carrying out the method according to the invention comprises an air main compressor, a two-stage rectification column and two heat exchange devices, the air main compressor being connected to the pressure stage of the rectification column via the first heat exchange device, while a second gas line is assigned to a second gas line, which is connected via the second heat exchange device and a relaxation machine is connected to the pressure stage, an oxygen extraction line from the low pressure stage via a pump through the second heat exchange device and is characterized in that the second gas line opens into two separate flow cross sections of the second heat exchange device, at least one of which contains another compressor, while the other is led at an intermediate point out of the second heat exchange device and is connected to an expansion machine, the output of which is connected to the rectification column.
  • the second heat exchange device has a plurality of heat exchanger blocks which are separate from one another, from which have a heat exchanger block flow cross sections for oxygen and the higher compressed part of the second gas stream, a second heat exchanger block flow cross sections for a partial flow of the higher compressed part of the second gas stream and a nitrogen flow from the rectification column, and a third heat exchanger block flow cross sections for the nitrogen flow from the second heat exchanger block and the contains lower compressed part of the second gas stream.
  • This arrangement has the advantage that the gas flows led through the second heat exchange device are largely decoupled from one another in terms of process, so that the temperature conditions in the individual heat exchanger blocks can be influenced. In this way, compressors, expansion machines and temperature differences on the heat exchangers can be optimized almost independently of one another.
  • FIGS 1 to 12 show different embodiments of the method according to the invention.
  • air 1 is turned into oxygen in a two-stage rectification column with a pressure stage 7 which is operated at a pressure of approximately 6 bar and a low pressure stage 15 which is operated at a pressure of approximately 1.5 bar. which is withdrawn in liquid form with a purity of about 99.5% via a line 16, impure nitrogen 17 from the top of the low pressure stage 15 and pure nitrogen 18 from the top of the pressure stage 7.
  • the two decomposition stages are connected to one another by a common condenser-evaporator and by connecting lines 19, 20.
  • the oxygen is brought to the desired delivery pressure, e.g. 70 bar, compressed.
  • the air 1 is first compressed to about 6 to 7 bar in an air main compressor 2, cooled in a spray zone cooler 3 and freed of CO 2 and H 2 0 in a couple of switchable molecular sieve adsorbers 4.
  • the air is then broken down into three partial flows: the largest partial flow 5 is exchanged in a first heat exchange device 6 in heat exchange with pure nitrogen 18 and with impure nitrogen 17, which has previously been preheated in heat exchange with the pre-separation products 19, 20 (heat exchanger 22, 23). cooled to about 100 K and fed to pressure stage 7.
  • a second partial stream 8 is further compressed in a compressor 9 to a pressure of approximately 75 bar and, after the compression heat has been removed, is cooled in a second heat exchange device 10 in heat exchange with evaporating product oxygen 16.
  • the pressure of the second partial stream 8 depends on the pressure of the oxygen to be evaporated. For reasons of heat balance, in order to prevent excessive temperature differences at the warm end of the first heat exchange device 6, part of the impure nitrogen 17 becomes in addition to the oxygen in the second heat exchange device 10 warmed up.
  • the second partial flow 8 is then expanded to the pressure of the pressure stage in a turbine 11 and also passed into the pressure stage 7.
  • a part of the cleaned air is post-compressed in a compressor 13 to a pressure of approximately 8 to 10 bar as the third partial flow 12 and cooled in the first heat exchange device 6 after the heat of compression has been removed.
  • a part of the third partial flow is removed at an intermediate point from the first heat exchange device 6 at a temperature of approx. 140 to 150 K, expanded in a work-performing manner (turbine 14) and introduced entirely or partially into the low-pressure stage 15 to improve the rectification.
  • the compressor 13 is coupled to the turbine 14 in order to transmit the turbine power.
  • the remaining part of the turbine stream is mixed with the impure nitrogen 17.
  • the addition takes place, as shown in the figure, after the heat exchangers 22, 23, but can also be carried out before or between these heat exchangers if necessary. Under certain conditions, it may also be more favorable to mix the entire turbine stream with the impure nitrogen 17.
  • the heat transfer enables the withdrawal of the third partial flow 12 for cooling in turbine 14, the withdrawal taking place approximately at the location of the first heat exchange device 6 at which the heat is supplied.
  • the first heat exchange device 6 there are large temperature differences at the ends and small ones in the middle with an excess of heated flows 17, 18.
  • the increased heating of: decomposition products in the first heat exchange device 6 further reduces the amount of air to be compressed in the compressor 9.
  • FIG. 3 shows an embodiment of the method according to the invention in which, as in FIG. 1, direct heat transfer takes place through line 24.
  • the second gas stream is compressed in two stages (compressors 9a and 9b).
  • the pressure after the compressor 9a is approx. 30 to 40 bar, after the compressor 9b approx. 75 bar.
  • a partial flow 28 is branched off between the compressors 9a, 9b, passed through part of the second heat exchange device 10 and removed therefrom at an intermediate point in the lower third.
  • This partial flow is expanded in a turbine 29 in a work-performing manner and, together with the higher compressed rest of the second air flow relaxed in the turbine 11, or (not shown) separately from this into the pressure stage 7.
  • the turbine 29 operates at a higher inlet temperature than the turbine 11. It therefore has a better cooling capacity and, moreover, does not work in the wet steam area.
  • the temperature differences at the cold end of the second heat exchange device 10 decrease, so that the energy losses during heat exchange are low.
  • FIG. 4 differs from the method according to FIG. 1 in that a part of the second air flow is expanded, instead of an intermediate pressure, as in FIG. 3, by the full final pressure of the compressor 9.
  • a partial flow 30 is branched off from the second air flow at an intermediate point of the second heat exchange device 10 and expanded in a turbine 31 while performing work. This partial flow is then introduced into the pressure stage 7 together with the remainder of the second air flow, which is relaxed in the turbine 11 or (not shown).
  • the second gas stream compressed to higher pressure is a nitrogen-rich gas stream 32 which is taken from the upper region of pressure stage 7.
  • the nitrogen 32 is partially heated in each of the two heat exchanger devices 6, 10 and then both partial streams are compressed together, nerêtr9) and cooled in heat exchange with liquid oxygen in the heat exchange device 10, relaxed during work (turbine 11) and, above the tapping point, into the pressure stage 7 returned.
  • heat is in turn transferred from the second to the first heat exchange device, specifically by means of a nitrogen flow 33, which branches off at an intermediate point of the heat exchange device 10 from the partial flow of nitrogen 32 passed through this heat exchange device and is mixed with the partial flow of nitrogen 32 passed through the heat exchange device 6 becomes.
  • the stream 33 can also be conducted to the warm end of the heat exchange device 6 independently of the partial stream 32.
  • Another nitrogen stream 36 is taken from the upper region of the low-pressure stage 15 and heated in the first heat exchange device 6.
  • the method according to FIG. 6 is analogous to that according to FIG. 2, but here, too, the second gas stream is a nitrogen stream 32 from the pressure stage 7.
  • the heat transfer according to the invention from the second heat exchange device 10 to the first heat exchange device 6 takes place by indirect heat exchange in a heat exchanger 25
  • a partial flow 34 of the compressed nitrogen 33 is branched off, cooled in the heat exchanger 25 and mixed with the rest of the nitrogen 33 emerging at the cold end of the heat exchange device 10.
  • the partial flow 34 is also expanded independently of the rest of the nitrogen 33 and passed to the pressure stage 7.
  • a part 35 is branched off, which absorbs heat from the partial flow 34 in the heat exchanger 25 and then supplies the part of the nitrogen 33 passed through the heat exchanger 6 at an intermediate point.
  • the partial flow 35 can instead (not shown) be conducted separately to the warm end of the heat exchange device 6.
  • FIG. 7 shows a variant of the method according to the invention, in which, in contrast to the method according to FIG. 2, the entire third partial stream 12 is expanded in the turbine 14.
  • the nitrogen 17 is led from the head of the low-pressure stage 15 only through the first heat exchange device 6, part of the nitrogen 17 being branched off in front of the heat exchange device 6 and fed to the heat exchange device 6 at an intermediate point after heat absorption in the heat exchanger 25 and together with the rest of nitrogen 17 is further heated.
  • the stream 27 can (not shown) also be conducted separately from the nitrogen 17 to the warm end of the heat exchange device 6.
  • the method according to FIG. 8 differs from that according to FIG. 7 only in that the second gas stream is nitrogen 32 from pressure stage 7.
  • the second gas stream is compressed in two compressor stages 9a and 9b.
  • air 101 is in a main air compressor 102 is compressed to about 6 bar, cooled in an Sprühzonenkühler 103 and 104 in the switchable Molekularsiebadsorbern of C02 H20 and freed.
  • the cleaned air is then divided into two air flows 105, 106.
  • the larger airflow 105 is cooled in a first heat exchange device 107 in heat exchange with nitrogen 119, 120 from the rectification and introduced into the pressure stage 108 of a two-stage rectification column.
  • the second air stream 106 is compressed to a higher pressure (approx.
  • the two stages of the rectification column are connected to one another by connecting lines 115, 116, nitrogen 119 from the top of the low-pressure stage is heated in heat exchangers 117, 118 in heat exchange with the pre-separation products 115, 116, these being simultaneously supercooled.
  • the nitrogen 119 is partly passed through the two heat exchangers 107, 111 and heated.
  • Nitrogen 120 from the top of the pressure stage 108 is heated in the heat exchange device 107.
  • the second air flow 106 is divided into two partial flows 121, 122 of different pressures.
  • the first partial flow 122 is the air flow which has already been mentioned and is compressed in the compressor 110.
  • the second partial flow 121 is formed by an air flow which is branched off between the two compressors 109, 110.
  • the air flow 121 is compressed in a compressor 123 from approximately 25 bar to a lower pressure than the air flow 122 compressed in the compressor 110 (approx. 33 bar) and cooled in the second heat exchange device 111.
  • the air flow 121 is removed from the heat exchange device 111, expanded in a turbine 124 to perform work and passed together with the air flow 105 into the pressure stage 108.
  • the removal takes place below the point at which the smallest temperature difference between the cold and warm flows prevails in the second heat exchange device 111.
  • the temperature at the inlet of the turbine 124 is, for example, 149 K, at the turbine 112, for example, 103 K.
  • the turbine 124 transfers its power to the compressor 123.
  • the cooling capacity of the turbine 124 covers approximately 80 to 90% of the cooling requirement of the system, that of the turbine 112 the rest.
  • part of the nitrogen 119 is branched off from the heat exchange device 111 at an intermediate point and fed to the nitrogen passed through the heat exchange device 107 at an intermediate point (line 125). With this measure, heat is transferred from the second to the first heat exchange device.
  • the method according to FIG. 10 differs from that according to FIG. 9 in the routing of the two air flows 121 and 122.
  • the same reference numerals as in FIG. 9 were used for the other, analog components.
  • the second partial air flow which was compressed to about 52 bar in the compressor 109, is partly (Air flow 121) cooled at this pressure in the second heat exchange device 111, removed from it at an intermediate point and relaxed in a turbine 124 to the pressure of the pressure stage 108, into which it is subsequently introduced together with the air flow 105.
  • the second partial flow 122 is compressed to a higher pressure (approx. 65 bar) in a compressor 110 and cooled in the second heat exchange device 111. At its cold end, the air flow 122 is removed, expanded in the turbine 112 to the pressure of the pressure stage 108 and introduced into it.
  • Turbine 124 is coupled to compressor 110. .
  • FIG. 11 shows an embodiment of the method according to the invention in which a recycle gas is provided as the second gas stream.
  • a gas stream 126 is taken from the rectification as the cycle gas.
  • the removal takes place in the lower region of pressure stage 108, i.e. the second gas stream has a composition similar to air.
  • a nitrogen-rich gas from the upper region of the pressure stage 108 as the recycle gas (dashed line).
  • the recycle gas 126 is warmed to approximately ambient temperature in the first heat exchange device 107, compressed in two compressors 109, 110, cooled in heat exchange with evaporating oxygen in the second heat exchange device 111, then expanded in the turbine 112 to perform work and passed into the pressure stage 108.
  • a portion 127 of the second gas stream is branched off upstream of the compressor 109, compressed to a pressure of approximately 6 to 10 bar in a compressor 128 and cooled in a portion of the first heat exchange device 107.
  • this gas flow is withdrawn, expanded to the pressure of the low-pressure stage 113 in a turbine 129 coupled to the compressor 128 and introduced into the latter.
  • the gas flow 127 is used for cooling.
  • a partial flow 121 is branched off between the two compressors 109, 110, post-compressed in a compressor 123 and cooled in part of the second heat exchange device 111.
  • the partial flow 121 is removed at a temperature prevailing over the cold end of the second heat exchange device 111, expanded to the pressure of the pressure stage in a turbine 124, which is coupled to the compressor 123, and admixed to the cycle gas 126.
  • FIG. 12 shows a method similar to that according to FIG. 9, in which the second heat exchange device is formed by three separate heat exchanger blocks 130, 131, 132. As a further difference, the connecting line 125 has been omitted.
  • the higher compressed partial flow 122 is cooled in the heat exchanger block 130 in heat exchange with evaporating oxygen.
  • a portion 133 of the stream 122 is removed at an intermediate point of the heat exchanger block 130 and cooled in the heat exchanger block 131 in heat exchange with a portion of the nitrogen 119 from the top of the low pressure stage 113, then together with the rest of the partial stream 122 cooled in the heat exchanger block 130 in the turbine 112 relaxed while working and passed to pressure stage 108.
  • the partial flow 121 branched off between the two compressors 109, 110 is cooled after it has been compressed in the compressor 123 in the heat exchanger block 132 in heat exchange with the partial flow of the nitrogen 119 preheated in the heat exchanger block 131, then in the turbine 124 relaxed while working and passed to pressure stage 108.
  • the air expanded in the turbine 124 can instead be directed to the low pressure stage 113 (dashed line).
  • the division of the heat exchange device 111 into three separate heat exchanger blocks 130, 131, 132 makes it possible to vary the pressures, amounts and temperatures of the air streams 121, 122 largely decoupled from one another at a predetermined oxygen delivery pressure and thus to select the optimal operating points of the compressors and turbine.
  • the inlet temperature at the turbine 124 can be selected independently of the temperature difference that must be maintained to evaporate the oxygen.
  • Figure 12 also shows in dash-dotted lines an additional embodiment of the method according to the invention, in which a part 134 of the compressed purified air 101 is compressed again in a compressor 135, branched off at an intermediate point from the first heat exchange device 107, relaxed in a turbine 136 and into the work Low pressure stage 113 is passed.

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Abstract

Bei einem Verfahren zur Gewinnung von gasförmigem Sauerstoff unter erhöhtem Druck durch Tieftemperaturrektifikation von Luft wird die Luft 1 zunächst komprimiert 2, dann gereinigt 3, 4 und mindestens zum Teil in einer ersten Wärmetauscheinrichtung 6 in Wärmetausch mit Zerlegungsprodukt abgekühlt und in die Rektifikation geleitet. Ein zweiter Gasstrom 8 wird auf einen höheren Druck verdichtet, in einer zweiten Wärmetauscheinrichtung 10 in Wärmetausch mit Zerlegungsprodukt abgekühlt, entspannt 11 und ebenfalls in die Rektifikation geleitet. Sauerstoff 16 wird in flüssiger Form aus der Rektifikation entnommen, auf den gewünschten Druck gepumpt und im Wärmetausch mit dem auf höheren Druck verdichteten Gasstrom 8 verdampft und angewärmt. Ein dritter Teilstrom 12 der zu zerlegenden Luft wird in Wärmetausch mit Zerlegungsprodukt abgekühlt.In a process for obtaining gaseous oxygen under elevated pressure by low-temperature rectification of air, the air 1 is first compressed 2, then cleaned 3, 4 and at least partially cooled in a first heat exchange device 6 in heat exchange with decomposition product and passed to the rectification. A second gas stream 8 is compressed to a higher pressure, cooled in a second heat exchange device 10 in heat exchange with decomposition product, expanded 11 and also passed into the rectification. Oxygen 16 is removed from the rectification in liquid form, pumped to the desired pressure and evaporated and heated in the heat exchange with the gas stream 8 compressed to higher pressure. A third partial flow 12 of the air to be separated is cooled in heat exchange with the decomposition product.

Description

Die Erfindung betrifft ein Verfahren zur Gewinnung von gasförmigem Sauerstoff unter erhöhtem Druck durch Tieftemperaturrektifikation von Luft, bei dem Luft komprimiert, gereinigt und mindestens zum Teil in einer ersten Wärmetauscheinrichtung in Wärmetausch mit Zerlegungsprodukt abgekühlt und in die Rektifikation geleitet wird, während ein zweiter Gasstrom auf einen höheren Druck verdichtet und in einer zweiten Wärmetauscheinrichtung in Wärmetausch mit Zerlegungsprodukt abgekühlt, entspannt und ebenfalls in die Rektifikation geleitet wird, und bei dem Sauerstoff zu flüssiger Form aus der Rektifikation entnommen, auf den gewünschten Druck gepumpt, in Wärmetausch mit dem auf höheren Druck verdichteten Gasstrom verdampft und angewärmt wird, sowie eine Vorrichtung zur Durchführung des Verfahrens.The invention relates to a process for the production of gaseous oxygen under elevated pressure by low-temperature rectification of air, in which air is compressed, cleaned and at least partially cooled in a first heat exchange device in heat exchange with decomposition product and passed into the rectification, while a second gas stream is passed onto one compressed higher pressure and cooled in a second heat exchange device in heat exchange with decomposition product, relaxed and also passed into the rectification, and in which oxygen is removed from the rectification in liquid form, pumped to the desired pressure, in heat exchange with the gas stream compressed to higher pressure is evaporated and heated, and a device for performing the method.

Ein derartiges Verfahren ist aus der DE-OS 25 57 453 bekannt. Der Sauerstoff wird flüssig aus der Rektifikation entnommen, in flüssiger Form auf den vom Verbraucher gewünschten erhöhten Druck komprimiert und anschließend verdampft und angewärmt. Unter erhöhtem Druck soll überatmosphärischer Druck verstanden werden. Die zur Verdampfung und Anwärmung des Sauerstoffes benötigte Wärmemenge wird von einem verdichteten Luftstrom geliefert. Aufgrund ihrer unterschiedlichen physikalischen Eigenschaften unterscheiden sich dieTemperaturverläufe von Sauerstoff und Luft.bei dem Wärmetausch. Es ergeben sich relativ große Temperaturdifferenzen am kalten Ende der zweiten Wärmetauscheinrichtung, was einen Energieverlust bedeutet.Such a method is known from DE-OS 25 57 453. The oxygen is withdrawn from the rectification in liquid form, compressed in liquid form to the increased pressure desired by the consumer and then evaporated and warmed up. Increased pressure should be understood to mean superatmospheric pressure. The evaporation and heating of the The amount of heat required for oxygen is supplied by a compressed air stream. Due to their different physical properties, the temperature profiles of oxygen and air differ during heat exchange. There are relatively large temperature differences at the cold end of the second heat exchange device, which means a loss of energy.

Diese unter der Bezeichnung "Innenverdichtung" bekannte Verfahrensweise zur Erzeugung von Sauerstoffgas unter Druck ist also energetisch relativ aufwendig. Sie hat jedoch gegenüber einem energetisch günstigeren Verfahren mit Außenverdichtung des Sauerstoffes, d.h. einem Verfahren, bei dem der Sauerstoff im wesentlichen drucklos und gasförmig aus der Rektifikation entnommen, angewärmt und auf den benötigten Abgabedruck verdichtet wird, den Vorteil, daß die Verdichtung von flüssigem Sauerstoff mit weit geringerem Brandrisiko durchgeführt werden kann.This procedure, known as "internal compression", for generating oxygen gas under pressure is therefore relatively expensive in terms of energy. However, compared to an energetically more favorable process with external compression of the oxygen, i.e. a process in which the oxygen is removed from the rectification in an essentially unpressurized and gaseous state, heated and compressed to the required delivery pressure, the advantage that the compression of liquid oxygen can be carried out with a far lower fire risk.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art zu entwickeln, bei dem der Energieverbrauch bei der Sauerstoffgewinnung verringert ist.The invention has for its object to develop a method of the type mentioned, in which the energy consumption in oxygen production is reduced.

Diese Aufgabe wird erfindungsgemäß dadurch gelöst, daß ein dritter Teilstrom des zu zerlegenden Gases in Wärmetausch mit Zerlegungsprodukt abgekühlt wird.This object is achieved in that a third partial stream of the gas to be decomposed is cooled in heat exchange with the decomposition product.

Bei einer bevorzugten Ausgestaltung des erfindungsgemäßen Verfahrens wird als dritter Gasstrom ein Teil der komprimierten gereinigten Luft in der ersten Wärmetauscheinrichtung abgekühlt, mindestens zum Teil an einer Zwischenstelle daraus entnommen und arbeitsleistend entspannt und wird von einer Zwischenstelle der zweiten Wärmetauscheinrichtung Wärme auf eine Zwischenstelle der ersten Wärmetauscheinrichtung übertragen.In a preferred embodiment of the method according to the invention, a part of the compressed, purified air is cooled in the first heat exchange device as a third gas stream, at least partially removed from it at an intermediate point and expanded to perform work, and heat is transferred from an intermediate point of the second heat exchange device to an intermediate point of the first heat exchange device .

Bei diesem Verfahren wird der Wärmeüberschuß, der am kalten Ende der zweiten Wärmetauscheinrichtung zur Verfügung steht, zur Kälteerzeugung ausgenutzt. Durch die Abführung von Wärme an einer Zwischenstelle der zweiten Wärmetauscheinrichtung wird die Temperaturdifferenz am kalten Ende verringert. Die entommene Wärmemenge wird der ersten Wärmetauscheinrichtung zugeführt, so daß dort im kalten Teil weniger Luft für die Anwärmung erforderlich ist.In this method, the excess heat, which at the cold end of the second heat exchange device Is available, used for refrigeration. The temperature difference at the cold end is reduced by the removal of heat at an intermediate point of the second heat exchange device. The amount of heat removed is fed to the first heat exchange device, so that less air is required for heating in the cold part.

Dieser eingesnarte Teil der eintretenden Luft wird bereits vor Beendigung seiner Abkühlung aus der ersten Wärmetauscheinrichtung entnonmen. Dieser als dritter Gasstrom bezeichnete Luft-Teilstrom wird arbeitsleistend entspannt, wobei Kälte erzeugt wird. Die Eintrittstemperatur bei der Entspannung ist durch die engste Temperaturdifferenz in der zweiten Wärmetauscheinrichtung bestimmt.This part of the air which has been cut in is removed from the first heat exchange device before it has cooled down. This partial air flow, referred to as the third gas flow, is expanded while performing work, with cooling being generated. The inlet temperature during expansion is determined by the narrowest temperature difference in the second heat exchange device.

. Bei einem Verfahren, bei dem als weiterer Produktstrom ein Niederdruck-Gasstrom aus der Rektifikation, insbesondere Stickstoff, zur Anwärmung durch die beiden Wärmetauscheinrichtungen geführt wird, kann durch die erfindungsgemäße Dereitstellung zusätzlicher Wärme in der ersten Wärmetauscheinrichtung dort eine größere Gasmenge zugunsten einer kleineren Gasmenge in der zweiten Wärmetauscheinrichtung durchgeleitet werden, so daß auch die Menge des zweiten Gasstroms in der zweiten Wärmetauscheinrichtung, welche auf einen relativ hohen Druck verdichtet wird, reduziert werden kann. Dadurch wird eine zusätzliche Energieeinsparung erzielt. Außerdem verringern sich durch die Verringerung der Mengenströme die Energieverluste am warmen Ende der zweiten Wärmetauscheinrichtung.. In a method in which a low-pressure gas stream from the rectification, in particular nitrogen, is passed through the two heat exchange devices as a further product stream, the provision of additional heat according to the invention in the first heat exchange device can result in a larger amount of gas in favor of a smaller amount of gas in the are passed through the second heat exchange device so that the amount of the second gas flow in the second heat exchange device, which is compressed to a relatively high pressure, can also be reduced. This results in additional energy savings. In addition, the energy losses at the warm end of the second heat exchange device are reduced by reducing the volume flows.

Gemäß einer vorteilhaften Weiterbildung des erfindungsgemäßen Verfahrens wird der dritte Gasstrom vor seiner Abkühlung weiterverdichtet.According to an advantageous development of the method according to the invention, the third gas stream is further compressed before it cools down.

Die Weiterverdichtung bringt einerseits ein größeres Druckgefälle und damit gleiche Kälteleistung bei geringerer Gasmenge, so daß der Hauptkompressor für die eintretende Luft verkleinert werden kann. Als weiterer Vorteil wird bei der Entspannung eine tiefere Endtemperatur erreicht, so daß die Ausbeute der Rektifikation verbessert wird.On the one hand, the further compression brings greater pressure slope and thus the same cooling capacity with a smaller amount of gas, so that the main compressor for the incoming air can be reduced. As a further advantage, a lower final temperature is reached during the expansion, so that the yield of the rectification is improved.

Zweckmäßigerweise wird der dritte Gasstrom nach seiner Entspannung in die Rektifikation und/oder in abziehenden Stickstoff aus der Rektifikation eingeleitet.The third gas stream is expediently introduced into the rectification and / or into the nitrogen withdrawn from the rectification after it has expanded.

Bei einer bevorzugten Ausgestaltung des erfindungsgemäßen Verfahrens wird der dritte Gasstrom im wesentlichen an der Stelle aus der ersten Wärmetauscheinrichtung entnommen, an der die Wärmezuführung erfolgt.In a preferred embodiment of the method according to the invention, the third gas stream is withdrawn from the first heat exchange device essentially at the point at which the heat is supplied.

Zur Lösung der gestellten Aufgabe erweist es sich weiterhin als günstig, gemäß einer Modifikation des Erfindungsgegenstandes den zweiten Teilstrom arbeitsleistend zu entspannen.In order to achieve the object, it has furthermore proven to be expedient to relax the second partial stream while working, according to a modification of the subject matter of the invention.

Die arbeitsleistende Entspannung bietet den Vorteil, daß weniger Luft am Luft-Hauptkompressor verdichtet werden muß. Alternativ kann die mit der arbeitsleistende Entspannung verbundene Mehrerzeugung an Kälte dazu genutzt werden, die Temperaturdifferenz am warmen und damit am kalten Ende der ersten und/oder zweiten Wärmetauscheinrichtung größer zu machen, so daß die Menge des zweiten Gasstroms verringert werden kann.The relaxation during work offers the advantage that less air has to be compressed on the main air compressor. Alternatively, the additional generation of cold associated with the work-performing relaxation can be used to make the temperature difference at the warm and thus at the cold end of the first and / or second heat exchange device larger, so that the amount of the second gas flow can be reduced.

In Weiterbildung des erfindungsgemäßen Verfahrens wird vorgeschlagen, daß zur Wärmeübertragung ein Teil des verdichteten zweiten Gasstroms vor Beendigung seiner Abkühlung in Wärmetausch mit einem Teil eines in der ersten Wärmetauscheinrichtung anzuwärmenden Gasstroms aus der Rektifikation abgekühlt wird.In a development of the method according to the invention, it is proposed that a portion of the compressed second gas stream is cooled in heat exchange with a portion of a gas stream to be heated in the first heat exchange device from the rectification before the end of its cooling.

Der Wärme abgebende zweite Teilstrom wird, je nach den Verfahrensbcdingungen, entweder dem verbliebenen Rest des zweiten Gasstroms, und zwar vorzugsweise nach dem Verlassen der zweiten wärmetauscheinrichtung, wieder zugeführt oder getrennt von diesem der Rektifikation zugeführt. Der Wärme aufnehmende Gasstrom wird nach der Wärmeaufnahme an einer Zwischenstelle in die erste Wärmetauscheinrichtung geführt und entweder zusammen mit dem restlichen Gasstrom, aus dem er entnommen wurde, oder getrennt von diesem, angewärmt.Depending on the process conditions, the heat-releasing second partial flow is either fed to the remaining part of the second gas flow, preferably after leaving the second heat exchange device, or fed separately from the latter to the rectification. After the heat has been absorbed, the heat-absorbing gas stream is conducted at an intermediate point into the first heat exchange device and heated either together with the remaining gas stream from which it was taken or separately from it.

Bei einer vorteilhaften Weiterbildung des erfindungsgemäßen Verfahrens wird die Verdichtung des zweiten Gasstroms in zwei Stufen durchgeführt, wobei zwischen den beiden Stufen ein Teilstrom abgezweigt, in der zweiten Wärmetauscheinrichtung abgekühlt und vor Beendigung des Wärmetausches arbeitsleistend entspannt und der Rektifikation zugeführt wird.In an advantageous development of the method according to the invention, the compression of the second gas stream is carried out in two stages, a partial stream being branched off between the two stages, cooled in the second heat exchange device and relaxed before the end of the heat exchange and carried out for rectification.

Die Aufsplittung des zweiten Gasstroms hat den Vorteil, daß die Eingangsdrücke an den Entspannungsmaschinen bei der arbeitsleistenden Entspannung der zwei Teilströme des zweiten Gasstroms jeweils optimiert werden können.The splitting of the second gas stream has the advantage that the inlet pressures on the expansion machines can be optimized in each case when the two partial streams of the second gas stream are depressurized.

Bei einer anderen vorteilhaften Ausgestaltung des Erfindungsgegenstandes wird ein Teil des auf seinen endgültigen Druck verdichteten zweiten Gasstroms vor Beendigung des Wärmetausches abgezweigt, arbeitsleistend entspannt und der Rektifikation zugeführt.In another advantageous refinement of the subject matter of the invention, a portion of the second gas stream compressed to its final pressure is branched off before the end of the heat exchange, expanded to perform work and fed to the rectification.

Der abgezweigte Teilstrom wird bei höherer Eintrittstemperatur entspannt als der am kalten Ende der zweiten Wärmetauscheinrichtung entnommene Rest des zweiten Gasstroms. Dadurch erhöht sich die Kälteleistung, außerdem. wird das Naßdampfgebiet bei der Entspannung vermieden. Als zusätzlicher Vorteil treten am kalten Ende der zweiten Wärmetauscheinrichtung kleine Temperaturdifferenzen auf.The branched partial stream is expanded at a higher inlet temperature than the rest of the second gas stream removed at the cold end of the second heat exchange device. This increases the cooling capacity, moreover. the wet steam area is avoided during relaxation. As an additional advantage, small temperature differences occur at the cold end of the second heat exchange device.

Es erweist sich als zweckmäßig, gemäß einer Weiterbildung des erfindungsgemäßen Verfahrens Stickstoff aus der Rektifikation jeweils zum Teil durch die erste und die zweite Wärmetauscheinrichtung zu führen und einen Teil des Stickstoffes von einer Zwischenstelle der zweiten Wärmetauscheinrichtung dem Stickstoff an einer Zwischenstelle der ersten Wärmetauscheinrichtung zuzuführen.It has proven to be expedient, in accordance with a development of the method according to the invention, to pass nitrogen from the rectification in part through the first and the second heat exchange device and to supply some of the nitrogen from an intermediate point of the second heat exchange device to the nitrogen at an intermediate point of the first heat exchange device.

Je nach Art des Verfahrens ist der zweite Gasstrom ein Teilstrom der zu zerlegenden Luft oder ein Gasstrom aus der Druckstufe.Depending on the type of process, the second gas flow is a partial flow of the air to be separated or a gas flow from the pressure stage.

Im ersteren Fall wird der zweite Gasstrom vor der ersten Wärmetauscheinrichtung abgezweigt. Im zweiten Fall wird ein Gasstrom aus der Druckstufe entnommen, dessen Stickstoffanteil gleich oder größer dem von Luft ist, in einer der beiden oder in Parallelführung in beiden Wärmetauscheinrichtungen angewärmt und anschließend verdichtet.In the former case, the second gas flow is branched off in front of the first heat exchange device. In the second case, a gas stream is taken from the pressure stage, the nitrogen content of which is equal to or greater than that of air, heated in one of the two or in parallel in both heat exchange devices and then compressed.

Zur Einsparung weiterer Energie wird vorgeschlagen, daß die bei der Entspannung des zweiten und/oder dritten Gasstroms gewonnene Arbeit zu dessen Nachverdichtung verwendet wird.To save further energy, it is proposed that the work obtained during the expansion of the second and / or third gas stream be used for its recompression.

Bei einer bevorzugten Weiterbildung des erfindungsgemäßen Verfahrens wird als dritter Teilstrom ein Teil des zweiten Gasstromes verwendet, wobei der zweite Gasstrom in zwei Teilströme aufgespaltet wird, die getrennt voneinander bei verschiedenen Drücken in der zweiten Wärmetauscheinrichtung abgekühlt werden, und daß der Teilstrom mit dem niedrigeren Druck bei einer höheren Temperatur als der Teilstrom mit dem höheren Druck aus der Wärmetauscheinrichtung entnommen, arbeitsleistend entspannt und in die Rektifikation geleitet wird.In a preferred development of the method according to the invention, part of the second gas flow is used as the third partial flow, the second gas flow being split into two partial flows, which are cooled separately from one another at different pressures in the second heat exchange device, and in that the partial flow with the lower pressure a higher temperature than the partial flow with the higher pressure is removed from the heat exchange device, relaxed during work and passed into the rectification.

Erfindungsgemäß wird der Hochdruckgasstrom, der zur Verdampfung des Sauerstoffes verwendet wird, in zwei Teilströme unterschiedlichen Druckes aufgeteilt, die getrennt voneinander durch die Wärmetauscheinrichtung geführt werden. Durch diese Maßnahme lassen sich ohne wesentliche Änderung der Kompressionsenergie Mengen und Drücke der beiden Teilströme variieren. Insbesondere können Druck und Menge des Teilstroms mit dem niedrigeren Druck so gewählt werden, daß seine arbeitsleistende Entspannung in Abhängigkeit von der durch den Sauerstoff-Abgabedruck festgelegten Eintrittstemperatur in die Entspannungsmaschine unter optimalen Bedingen abläuft, d.h. in einem Druckbereich, in dem das Lcistungsmaximum liegt. Gleichzeitig wird durch die erfindungsgemäß vorzeitige Entnahme des Teilstroms mit dem niedrigeren Druck der. Wärmeüberschuß, der am kalten Ende der zweiten Wärmetauscheinrichtung herrscht, und damit der Energieverlust, verringert. Der Druck des höher verdichteten Teilstroms ist in weiten Grenzen variierbar, dadurch ist auch der Sauerstoff-Abgabedruck in weiten Grenzen variierbar.According to the invention, the high-pressure gas stream which is used to evaporate the oxygen is divided into two sub-streams of different pressure, which are passed separately through the heat exchange device. This measure allows the quantities and pressures of the two partial flows to be varied without a significant change in the compression energy. In particular, the pressure and quantity of the partial flow with the lower pressure can be selected so that its work-relieving expansion takes place under optimal conditions, depending on the inlet temperature into the expansion machine determined by the oxygen delivery pressure, i.e. in a pressure range in which the performance maximum lies. At the same time, due to the early removal of the partial flow with the lower pressure according to the invention. Excess heat, which prevails at the cold end of the second heat exchange device, and thus the energy loss, is reduced. The pressure of the higher compressed partial flow can be varied within wide limits, which means that the oxygen delivery pressure can also be varied within wide limits.

Gemäß einer Ausgestaltung des erfindungsgemäßen Verfahrens wird der auf höherem Druck befindliche Teilstrom nach seiner Abkühlung arbeitsleistend entspannt. Dabei wird die Kompressionsenergie optimal genutzt. Die hohe Kälteleistung durch die getrennte Entspannung der beiden Teilströme ermöglicht relativ große Temperaturdifferenzen an den warmen Enden der Wärmetauscheinrichtungen, wodurch die notwendige Menge verdichteter Luft niedrig gehalten werden kann. Weiter entfällt die Verdichtung zusätzlicher Luft zur Kälteerzeugung, d.h. die Gesamtluftmenge wird in Abhängigkeit von den gewünschten Zerlegungsprodukten ein Minimum. Als Folge davon sind der Luft-Hauptkompressor und die Reinigungsstufe so klein wie möglich dimensioniert.According to one embodiment of the method according to the invention, the partial flow at a higher pressure is relieved of work after its cooling. The compression energy is used optimally. The high cooling capacity due to the separate expansion of the two partial flows enables relatively large temperature differences at the warm ends of the heat exchange devices, as a result of which the necessary amount of compressed air can be kept low. Furthermore, there is no compression of additional air for cooling, i.e. the total amount of air becomes a minimum depending on the desired decomposition products. As a result, the main air compressor and cleaning stage are dimensioned as small as possible.

Es ist zweckmäßig, wenn der Teilstrom mit dem niedrigeren Druck nach Austritt aus der ersten Verdichterstufe vor seiner Abkühlung nachverdichtet wird. Dies hat den Zweck, die bei der Entspannung freiwerdende Energie optimal zu nutzen und damit den Energiebedarf zur Verdichtung auf den gewählten Druck niedrig zu halten. Der andere der beiden Teilströme, der erfindungsgemäß mit einem höheren Druck durch die Wärmetauscheinrichtung geführt wird, wird in der folgenden Verdichterstufe weiterverdichtet. Druck und Durchsatzmengen lassen sich dabei an den Verdichtern so einstellen, daß die Verdichter im optimalen Arbeitspunkt betrieben werden können, weil Luft und Sauerstoff nur indirekt miteinander gekoppelt sind. Dieser Vorteil gilt vor allem auch im Teillastbetrieb bei unverändert hohem Sauerstoffabgabedruck.It is useful if the partial flow with the lower Pressure after leaving the first compressor stage is recompressed before it cools down. The purpose of this is to optimally use the energy released during relaxation and thus to keep the energy required for compression to the selected pressure low. The other of the two partial flows, which according to the invention is led through the heat exchange device at a higher pressure, is further compressed in the following compressor stage. Pressure and flow rates can be set on the compressors so that the compressors can be operated at the optimum operating point because air and oxygen are only indirectly linked to one another. This advantage applies especially in part-load operation with an unchanged high oxygen delivery pressure.

Der Druck des. Teilstroms mit dem niedrigeren Druck beträgt. gemäß einer Ausgestaltung des erfindungsgemäßen Verfahrens. zwischen 10 bar und 60 bar. Der bevorzugte Druckbereich liegt zwischen 20 und 40 bar. Der jeweilige Druck hängt vom Druck des Sauerstoffs ab.The pressure of the partial flow with the lower pressure is. according to an embodiment of the method according to the invention. between 10 bar and 60 bar. The preferred pressure range is between 20 and 40 bar. The respective pressure depends on the pressure of the oxygen.

Es erweist sich als vorteilhaft, wenn gemäß einer bevorzugten Ausgestaltung des erfindungsgemäßen Verfahrens der Teilstrom mit dem niedrigeren Druck im Bereich der gerinsten Temperaturdifferenz zwischen dem Teilstrom mit dem höheren Druck und dem Sauerstoff aus der zweiten Wärmetauscheinrichtung entnommen wird.It proves to be advantageous if, according to a preferred embodiment of the method according to the invention, the partial flow with the lower pressure in the region of the lowest temperature difference between the partial flow with the higher pressure and the oxygen is removed from the second heat exchange device.

Aufgrund der eingangs erwähnten physikalischen Gegebenheiten ist die Temperaturdifferenz am Ende der zweiten Wärmetauscheinrichtung relativ groß und und nimmt an einer Zwischenstelle der Wärmetauscheinrichtung ein Minimum an. Dies ist die bevorzugte Entnahmestelle für den niedriger verdichteten Teilstrom. Durch die Entnahme des warmen Gases verkleinert sich die Temperaturdifferenz am kalten Ende der Wärmetauscheinrichtung und damit der Energiebedarf des Verfahrens.Due to the physical conditions mentioned at the outset, the temperature difference at the end of the second heat exchange device is relatively large and assumes a minimum at an intermediate point of the heat exchange device. This is the preferred point of withdrawal for the lower compressed partial flow. By removing the warm gas, the temperature difference at the cold end of the heat exchange device is reduced, and thus the energy requirement of the Procedure.

Bei einer bevorzugten Weiterbildung des Erfindungsgegenstandes wird die bei der Entspannung des einen der beiden und/ oder beider Teilströme geleistete Arbeit für eine Nachverdichtung des einen der beiden oder beider Teilströme verwendet. Die Koppelung einer oder beider Entspannungsmaschinen mit einem oder beiden Nachverdichtern verringert den Energieeinsatz.In a preferred development of the subject matter of the invention, the work performed in relieving the pressure on one of the two and / or both partial flows is used for post-compression of the one or both partial flows. Coupling one or both expansion machines with one or both post-compressors reduces energy consumption.

Gemäß einer vorteilhaften Ausgestaltung des Erfindungsgegenstandes wird Wärme von einer Zwischenstelle der einen auf eine Zwischenstelle der anderen Wärmetauscheinrichtung übertragen. Der Wärmetausch erfolgt entweder indirekt oder durch direkte Uberführung eines Gasstroms von der einen in die andere Wärmetauscheinrichtung. Diese Maßnahme erweist sich als sehr effektvoll, um die Temperaturdifferenzen an den Wärmetauscheinrichtungen zu optimieren.According to an advantageous embodiment of the subject matter of the invention, heat is transferred from an intermediate point of one to an intermediate point of the other heat exchange device. The heat exchange takes place either indirectly or by direct transfer of a gas flow from one to the other heat exchange device. This measure proves to be very effective in order to optimize the temperature differences at the heat exchange devices.

In weiterer Ausgestaltung des Erfindungsgegenstandes wird vorgeschlagen, daß ein Teil der komprimierten, gereinigten Luft an einer Zwischenstelle der ersten Wärmetauscheinrichtung abgezweigt, arbeitsleistend entspannt und.in die Rektifikation geleitet wird. Damit wird die Kälteleistung erhöht, falls die Kälteleistung aus der Entspannung des Mittel- und Hochdruckstromes nicht ausreichen sollte.In a further embodiment of the subject matter of the invention, it is proposed that a portion of the compressed, purified air be branched off at an intermediate point of the first heat exchange device, relaxed in order to perform work, and passed into the rectification. This increases the cooling capacity if the cooling capacity from the expansion of the medium and high pressure flow is insufficient.

Insbesondere ist es hierbei von Vorteil, wenn der abgezweigte Teil der Luft vor seiner Abkühlung nachverdichtet wird.It is particularly advantageous here if the branched-off part of the air is post-compressed before it is cooled.

Der zweite Gasstrom ist vorzugsweise ein Teilstrom der eintretenden Luft.The second gas stream is preferably a partial stream of the incoming air.

Bei einer anderen vorteilhaften Weiterbildung des Erfin- . dungsgegenstandes wird der zweite Gasstrom aus der Druckstufe entnommen und vor seiner Aufspaltung angewärmt und verdichtet. Diese Gasstrom ist entweder ein Gasstrom aus dem unteren Bereich der Druckstufe mit einer Zusammensetzung etwa wie Luft, oder aber ein stickstoffreicher Gasstrom aus dem oberen Bereich der Druckstufe.In another advantageous development of the inventor. the second gas flow from the pressure removed stage and warmed and compressed before its splitting. This gas stream is either a gas stream from the lower region of the pressure stage with a composition such as air, or a nitrogen-rich gas stream from the upper region of the pressure stage.

In weiterer Ausgestaltung der letztgenannten Weiterbildung des erfindungsgemäßen Verfahrens wird ein Teil des zweiten Gasstroms vor seiner Verdichtung nachverdichtet, in einer der Wärmetauscheinrichtungen abgekühlt, an einer Zwischenstelle daraus entnommen, arbeitsleistend entspannt und in die Rektifikation geleitet.In a further embodiment of the last-mentioned further development of the method according to the invention, a part of the second gas stream is post-compressed before it is compressed, cooled in one of the heat exchange devices, removed from it at an intermediate point, expanded in a work-performing manner and passed into the rectification.

Eine Vorrichtung zur Durchführung des erfindungsgemäßen Verfahrens umfaßt einen Luft-Hauptkompressor, eine zweistufige Rektifiziersäule sowie zwei Wärmetauscheinrichtungen, wobei der Luft-Hauptkompressor über die erste Wärmetauscheinrichtung mit der Druckstufe der Rektifziersäule verbunden ist, während einer zweiten Gasleitung ein zweiter Verdichter zugeordnet ist, der über die zweite Wärmetauscheinrichtung und eine Entspannungsmaschine mit der Druckstufe verbunden ist, wobei eine Sauerstoff-Entnahmeleitung aus der Niederdruckstufe über eine Pumpe durch die zweite Wärmetauscheinrichtung führt und ist dadurch gekennzeichnet, daß die zweite Gasleitung in zwei separate Strömungsquerschnitte der zweiten Wärmetauscheinrichtung mündet, von denen zumindest eine einen weiteren Verdichter enthält, während die andere an-einer Zwischenstelle aus der zweiten Wärmetauscheinrichtung geführt und mit einer Entspannungsmaschine verbunden ist, deren Ausgang mit der Rektifiziersäule in Verbindung steht.A device for carrying out the method according to the invention comprises an air main compressor, a two-stage rectification column and two heat exchange devices, the air main compressor being connected to the pressure stage of the rectification column via the first heat exchange device, while a second gas line is assigned to a second gas line, which is connected via the second heat exchange device and a relaxation machine is connected to the pressure stage, an oxygen extraction line from the low pressure stage via a pump through the second heat exchange device and is characterized in that the second gas line opens into two separate flow cross sections of the second heat exchange device, at least one of which contains another compressor, while the other is led at an intermediate point out of the second heat exchange device and is connected to an expansion machine, the output of which is connected to the rectification column.

Eine Weiterbildung dieser Vorrichtung ist dadurch gekennzeichnet, daß die zweite Wärmetauscheinrichtung mehrere voneinander getrennte Wärmetauscherblöcke aufweist, von denen ein Wärmetauscherblock Strömungsquerschnitte für Sauerstoff und den höher verdichteten Teil des zweiten Gasstroms, ein zweiter Wärmetauscherblock Strömungsquerschnitte für einen Teilstrom des höher verdichteten Teils des zweiten Gasstroms und einen Stickstoffstrom aus der Rektifiziersäule, sowie ein dritter Wärmetauscherblock Strömungsquerschnitte für den Stickstoffstrom aus dem zweiten Wärmetauscherblock und den niedriger verdichteten Teil des zweiten Gasstroms enthält.A further development of this device is characterized in that the second heat exchange device has a plurality of heat exchanger blocks which are separate from one another, from which have a heat exchanger block flow cross sections for oxygen and the higher compressed part of the second gas stream, a second heat exchanger block flow cross sections for a partial flow of the higher compressed part of the second gas stream and a nitrogen flow from the rectification column, and a third heat exchanger block flow cross sections for the nitrogen flow from the second heat exchanger block and the contains lower compressed part of the second gas stream.

Diese Anordnung weist den Vorteil auf, daß die durch die zweite Wärmetauscheinrichtung geführten Gasströme verfahrensmäßig weitgehend voneinander entkoppelt sind, so daß die Temperaturverhältnisse in den einzelnen Wärmetauscherblöcken beeinflußbar sind. Auf diese Weise lassen sich Verdichter, Entspannungsmaschinen und Temperaturdifferenzen an den Wärmetauschern nahezu unabhängig voneinander optimieren.This arrangement has the advantage that the gas flows led through the second heat exchange device are largely decoupled from one another in terms of process, so that the temperature conditions in the individual heat exchanger blocks can be influenced. In this way, compressors, expansion machines and temperature differences on the heat exchangers can be optimized almost independently of one another.

Mit dem erfindungsgemäßen Verfahren ist es möglich, den Energieverbrauch bei der Innenverdichtung von Sauerstoff größenordnungsmäßig auf denjenigen bei der Außenverdichtung abzusenken.With the method according to the invention, it is possible to reduce the energy consumption in the internal compression of oxygen by an order of magnitude to that in the external compression.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden anhand von schematisch dargestellten Ausführungsbeispielen näher erläutert.The invention and further details of the invention are explained in more detail with reference to schematically illustrated exemplary embodiments.

Hierbei zeigen die Figuren 1 bis 12 verschiedene Ausführungsformen des erfindungsgemäßen Verfahrens.Figures 1 to 12 show different embodiments of the method according to the invention.

Bei dem Verfahren gemäß Figur 1 wird Luft 1 in einer zweistufigen Rektifiziersäule mit einer Druckstufe 7, die bei einem Druck von etwa 6 bar betrieben wird und einer Niederdruckstufe 15, die bei einem Druck von ca. 1,5 bar betrieben wird, in Sauerstoff, der mit ca. 99,5% Reinheit über eine Leitung 16 flüssig entnommen wird, unreinen Stickstoff 17 vom Kopf der Niederdruckstufe 15 und reinen Stickstoff 18 vom Kopf der Druckstufe 7 zerlegt. Die beiden Zerlegungsstufen sind durch einen gemeinsamen Kondensator-Verdampfer sowie durch Verbindungsleitungen 19,20 miteinander verbunden. Der Sauerstoff wird mittels einer Pumpe 21 in flüssigem Zustand auf den gewünschten Abgabedruck, z.B. 70 bar, verdichtet.In the process according to FIG. 1, air 1 is turned into oxygen in a two-stage rectification column with a pressure stage 7 which is operated at a pressure of approximately 6 bar and a low pressure stage 15 which is operated at a pressure of approximately 1.5 bar. which is withdrawn in liquid form with a purity of about 99.5% via a line 16, impure nitrogen 17 from the top of the low pressure stage 15 and pure nitrogen 18 from the top of the pressure stage 7. The two decomposition stages are connected to one another by a common condenser-evaporator and by connecting lines 19, 20. The oxygen is brought to the desired delivery pressure, e.g. 70 bar, compressed.

Die Luft 1 wird zunächst in einem Luft-Hauptkompressor 2 auf etwa 6 bis 7 bar verdichtet, in einem Sprühzonenkühler 3 abgekühlt und in einem paar von umschaltbaren Molsiebadsorbern 4 von CO2 und H20 befreit. Die Luft wird anschließend in drei Teilströme zerlegt: Der größte Teilstrom 5 wird in einer ersten Wärmetauscheinrichtung 6 in Wärmetausch mit reinem Stickstoff 18 sowie mit unreinem Stickstoff 17, der zuvor in Wärmetausch mit den Vorzerlegungsprodukten 19, 20 vorgewärmt worden ist (Wärmetauscher 22,23) auf etwa 100 K abgekühlt und der Druckstufe 7 zugeführt.The air 1 is first compressed to about 6 to 7 bar in an air main compressor 2, cooled in a spray zone cooler 3 and freed of CO 2 and H 2 0 in a couple of switchable molecular sieve adsorbers 4. The air is then broken down into three partial flows: the largest partial flow 5 is exchanged in a first heat exchange device 6 in heat exchange with pure nitrogen 18 and with impure nitrogen 17, which has previously been preheated in heat exchange with the pre-separation products 19, 20 (heat exchanger 22, 23). cooled to about 100 K and fed to pressure stage 7.

Ein zweiter Teilstrom 8 wird in einem Verdichter 9 auf einen Druck von ca. 75 bar weiterverdichtet und nach Abführung der Kompressionswärme in einer zweiten Wärmetauscheinrichtung 10 in Wärmetausch mit verdampfendem Produktsauerstoff 16 abgekühlt. Der Druck des zweiten Teilstroms 8 hängt vom Druck des zu verdampfenden Sauerstoffes ab. Aus Wärmebilanzgründen, um zu große Temperaturdifferenzen am warmen Ende der ersten Wärmetauscheinrichtung 6 zu verhindern, wird ein Teil des unreinen Stickstoffes 17 zusätzlich zum Sauerstoff in der zweiten Wärmetauscheinrichtung 10 angewärmt. Der zweite Teilstrom 8 wird dann in einer Turbine 11 arbeitsleistend auf den Druck der Druckstufe entspannt und ebenfalls in die Druckstufe 7 geleitet.A second partial stream 8 is further compressed in a compressor 9 to a pressure of approximately 75 bar and, after the compression heat has been removed, is cooled in a second heat exchange device 10 in heat exchange with evaporating product oxygen 16. The pressure of the second partial stream 8 depends on the pressure of the oxygen to be evaporated. For reasons of heat balance, in order to prevent excessive temperature differences at the warm end of the first heat exchange device 6, part of the impure nitrogen 17 becomes in addition to the oxygen in the second heat exchange device 10 warmed up. The second partial flow 8 is then expanded to the pressure of the pressure stage in a turbine 11 and also passed into the pressure stage 7.

Erfindungsgemäß wird als dritter Teilstrom 12 ein Teil der gereinigten Luft in einem Verdichter 13 auf einen Druck von ca. 8 bis 10 bar nachverdichtet und nach Abführung der Kompressionswärme in der ersten Wärmetauscheinrichtung 6 abgekühlt. Ein Teil des dritten Teilstroms wird an einer Zwischenstelle aus der ersten Wärmetauscheinrichtung 6 bei einer Temperatur von ca. 140 bis 150 K entnommen, arbeitsleistend entspannt (Turbine 14) und zur Verbesserung der 'Rektifikation ganz oder teilweise in die Niederdruckstufe 15 eingeleitet. Der Verdichter 13 ist zur übertragung der Turbinenleistung mit der Turbine 14 gekoppelt. Der restliche Teil des Turbinenstroms wird dem unreinen Stickstoff 17 beigemischt. Die Zumischung erfolgt, wie in der Figur dargestellt, nach den Wärmetauschern 22, 23, kann aber bei Bedarf auch vor oder zwischen diesen Wärmetauschern vorgenommen werden. Auch kann es unter gewissen Voraussetzungen günstiger sein, den gesamten Turbinenstrom dem unreinen Stickstoff 17 beizumischen.According to the invention, a part of the cleaned air is post-compressed in a compressor 13 to a pressure of approximately 8 to 10 bar as the third partial flow 12 and cooled in the first heat exchange device 6 after the heat of compression has been removed. A part of the third partial flow is removed at an intermediate point from the first heat exchange device 6 at a temperature of approx. 140 to 150 K, expanded in a work-performing manner (turbine 14) and introduced entirely or partially into the low-pressure stage 15 to improve the rectification. The compressor 13 is coupled to the turbine 14 in order to transmit the turbine power. The remaining part of the turbine stream is mixed with the impure nitrogen 17. The addition takes place, as shown in the figure, after the heat exchangers 22, 23, but can also be carried out before or between these heat exchangers if necessary. Under certain conditions, it may also be more favorable to mix the entire turbine stream with the impure nitrogen 17.

Aufgrund der hohen spezifischen Wärme von Luft unterhalb des kritischen Punktes steht am kalten Ende der zweiten Wärmetauscheinrichtung 10 eine große Wärmemenge zur Anwärmung einer entsprechenden Menge unreinen Stickstoffes 17 zur Verfügung. Nach Anwärmung im unteren Drittel der zweiten Wärmetauscheinrichtung 10 wird gemäß einem weiteren Erfindungsmerkmal durch Abzweigung eines Teils des Stickstoffes 17 in Leitung 24 Wärme aus der zweiten Wärmetauscheinrichtung 10 auf eine Zwischenstelle der ersten Wärmetauscheinrichtung 6 übertragen. Der durch Leitung 24 geführte Gasstrom wird, wie im gezeigten Beispiel, mit dem durch die erste Wärmetauscheinrichtung 6 geführten Teilstrom des unreinen Stickstoffes 17 vermischt und zusammen mit diesem oder aber (nicht dargestellt) getrennt davon angewärmt.Due to the high specific heat of air below the critical point, a large amount of heat is available at the cold end of the second heat exchange device 10 for heating a corresponding amount of impure nitrogen 17. After heating in the lower third of the second heat exchange device 10, according to a further feature of the invention, heat is transferred from the second heat exchange device 10 to an intermediate point of the first heat exchange device 6 by branching off part of the nitrogen 17 in line 24. The gas flow led through line 24 is, as in the example shown, with that led through the first heat exchange device 6 Partial stream of the impure nitrogen 17 mixed and heated together with this or (not shown) separately.

Je kleiner die Menge des in der zweiten Wärmetauscheinrichtung 10 zu erwärmenden Stickstoffes 17 ist, desto weniger Luft muß im Verdichter 9 verdichtet werden. Gleichzeitig ermöglicht die Wärmeübertragung den Abzug des dritten Teilstroms 12 zur Kälteerzeugung in Turbine 14, wobei der Abzug etwa an der Stelle der ersten Wärmetauscheinrichtung 6 erfolgt, an der die Wärme zugeführt wird. In der ersten Wärmetauscheinrichtung 6 ergeben sich große Temperaturdifferenzen an den Enden und kleine in der Mitte bei einem Uberschuß an angewärmten Strömen 17, 18. Durch die vermehrte Anwärmung von:Zerlegungsprodukten in der ersten Wärmetauscheinrichtung 6 wird die im Verdichter 9 zu verdichtende Luftmenge weiter verringert.The smaller the amount of nitrogen 17 to be heated in the second heat exchange device 10, the less air has to be compressed in the compressor 9. At the same time, the heat transfer enables the withdrawal of the third partial flow 12 for cooling in turbine 14, the withdrawal taking place approximately at the location of the first heat exchange device 6 at which the heat is supplied. In the first heat exchange device 6 there are large temperature differences at the ends and small ones in the middle with an excess of heated flows 17, 18. The increased heating of: decomposition products in the first heat exchange device 6 further reduces the amount of air to be compressed in the compressor 9.

Bei der Ausführungsform des erfindungsgemäßen Verfahrens gemäß Figur 2, bei der, wie auch bei den übrigen Figuren, für analoge Anlagenteile dieselben Bezugszeichen verwendet sind, wird im Unterschied zu dem Verfahren gemäß Figur 1 anstelle einer direkten Wärmeübertragung zwischen den beiden Wärmetauscheinrichtungen 6,.10 ein indirekter Wärmetausch in einem Wärmetauscher 25 durchgeführt. Hierbei wird im unteren Drittel der zweiten Wärmetauscheinrichtung 10 ein Teilstrom 26 des zweiten Luftstroms entnommen und in Wärmetausch mit einem Teilstrom 27 des Stickstoffs 17 gebracht, der anschließend der ersten Wärmetauscheinrichtung 6 an einer Zwischenstelle zugeführt wird. Der Teilstrom 26 wird dem restlichen zweiten Luftstrom 8 vor dessen Entspannung wieder zugeführt oder (nicht dargestellt) direkt in die Druckstufe 7 geführt. Der Teilstrom 27 wird dem Stickstoff 17 zugemischt und gemeinsam oder (nicht dargestellt) getrennt von diesem zum warmen Ende der Wärmetauscheinrichtung 6 geführt.In the embodiment of the method according to the invention according to FIG. 2, in which, like in the other figures, the same reference numerals are used for analog system parts, in contrast to the method according to FIG. 1, instead of a direct heat transfer between the two heat exchange devices 6, .10 indirect heat exchange carried out in a heat exchanger 25. In the lower third of the second heat exchange device 10, a partial flow 26 of the second air flow is removed and brought into heat exchange with a partial flow 27 of nitrogen 17, which is then fed to the first heat exchange device 6 at an intermediate point. The partial flow 26 is fed back to the remaining second air flow 8 before it is released or led (not shown) directly into the pressure stage 7. The partial stream 27 is mixed with the nitrogen 17 and together or (not shown) separately from this to the warm end of the heat exchanger tung 6 led.

Figur 3 zeigt eine Ausführungsform des erfindungsgemäßen Verfahrens, bei der, wie bei Figur 1., eine direkte Wärmeübertragung durch Leitung 24 stattfindet. Im Unterschied dazu wird der zweite Gasstrom in zwei Stufen (Verdichter 9a und 9b) verdichtet. Der Druck nach dem Verdichter 9a beträgt ca. 30 bis 40 bar, nach dem Verdichter 9b ca. 75 bar. Zwischen den Verdichtern 9a, 9b wird ein Teilstrom 28 abgezweigt, durch einen Teil der zweiten Wärmetauscheinrichtung 10 geführt und an einer Zwischenstelle im unteren Drittel daraus entnommen. Dieser Teilstrom wird in einer Turbine 29 arbeitsleistend entspannt und gemeinsam mit dem in der Turbine 11 entspannten höher verdichteten Rest des zweiten Luftstroms oder (nicht dargestellt) getrennt von diesem in die Druckstufe 7 geführt. Die Turbine 29 arbeitet bei höherer Eintrittstemperatur als die Turbine 11. Sie weist daher eine bessere Kälteleistung auf und arbeitet außerdem nicht im Naßdampfgebiet. Als weiterer Vorteil verringern sich die Temperaturdifferenzen am kalten Ende der zeiten Wärmetauscheinrichtung 10, so daß die Energieverluste beim Wärmetausch gering sind.FIG. 3 shows an embodiment of the method according to the invention in which, as in FIG. 1, direct heat transfer takes place through line 24. In contrast, the second gas stream is compressed in two stages (compressors 9a and 9b). The pressure after the compressor 9a is approx. 30 to 40 bar, after the compressor 9b approx. 75 bar. A partial flow 28 is branched off between the compressors 9a, 9b, passed through part of the second heat exchange device 10 and removed therefrom at an intermediate point in the lower third. This partial flow is expanded in a turbine 29 in a work-performing manner and, together with the higher compressed rest of the second air flow relaxed in the turbine 11, or (not shown) separately from this into the pressure stage 7. The turbine 29 operates at a higher inlet temperature than the turbine 11. It therefore has a better cooling capacity and, moreover, does not work in the wet steam area. As a further advantage, the temperature differences at the cold end of the second heat exchange device 10 decrease, so that the energy losses during heat exchange are low.

Die in Figur 4 gezeigte Ausführungsform des erfindungsgemäßen Verfahrens unterscheidet sich von dem Verfahren gemäß Figur 1 dadurch, daß ein Teil des zweiten Luftstroms statt von einem Zwischendruck - wie bei Figur 3 - von dem vollen Enddruck des Verdichters 9 entspannt wird. Von dem zweiten Luftstrom wird an einer Zwischenstelle der zweiten Wärmetauscheinrichtung 10 ein Teilstrom 30 abgezweigt und in einer Turbine 31 arbeitsleistend entspannt. Anschließend wird dieser Teilstrom zusammen mit dem in der Turbine 11 entspannten Rest des zweiten Luftstroms oder (nicht dargestellt) getrennt von diesem in die Druckstufe 7 eingeleitet..The embodiment of the method according to the invention shown in FIG. 4 differs from the method according to FIG. 1 in that a part of the second air flow is expanded, instead of an intermediate pressure, as in FIG. 3, by the full final pressure of the compressor 9. A partial flow 30 is branched off from the second air flow at an intermediate point of the second heat exchange device 10 and expanded in a turbine 31 while performing work. This partial flow is then introduced into the pressure stage 7 together with the remainder of the second air flow, which is relaxed in the turbine 11 or (not shown).

Ein analoges Verfahren zur Figur 1 zeigt die Figur 5, allerdings mit dem Unterschied, daß der auf höheren Druck verdichtete zweite Gasstrom ein stickstoffreicher Gasstrom 32 ist, der aus dem oberen Bereich der Druckstufe 7 entnommen wird. Der Stickstoff 32 wird jeweils zum Teil in den beiden Wärmetauschereinrichtungen 6, 10 angewärmt und anschließend beide Teilströme gemeinsam verdichtet Nerdichter9) und in Wärmetausch mit flüssigem Sauerstoff in der Wärmetauscheinrichtung 10 abgekühlt, arbeitsleistend entspannt (Turbine 11) und, oberhalb der Entnahmestelle, in die Druckstufe 7 zurückgeleitet. Erfindungsgemäß wird wiederum Wärme von der zweiten auf die erste Wärmetauscheinrichtung übertragen und zwar durch einen Stickstoffstrom 33, der an einer Zwischenstelle der Wärmetauscheinrichtung 10 von dem durch diese Wärmetauscheinrichtung geführten Teilstrom des Stickstoffes 32 abgezweigt und mit dem durch die Wärmetauscheinrichtung 6 geführten Teilstrom des Stickstoffes 32 vermischt wird. Stattdessen kann (nicht dargestellt) der Strom 33 auch unabhängig von dem Teilstrom 32 zum warmen Ende der Wärmetauscheinrichtung 6 geführt werden. Ein weiterer Stickstoffstrom 36 wird aus dem oberen Bereich der Niederdruckstufe 15 entnommen und in der ersten Wärmetauscheinrichtung 6 angewärmt.5 shows an analogous method to FIG. 1, but with the difference that the second gas stream compressed to higher pressure is a nitrogen-rich gas stream 32 which is taken from the upper region of pressure stage 7. The nitrogen 32 is partially heated in each of the two heat exchanger devices 6, 10 and then both partial streams are compressed together, nerdichter9) and cooled in heat exchange with liquid oxygen in the heat exchange device 10, relaxed during work (turbine 11) and, above the tapping point, into the pressure stage 7 returned. According to the invention, heat is in turn transferred from the second to the first heat exchange device, specifically by means of a nitrogen flow 33, which branches off at an intermediate point of the heat exchange device 10 from the partial flow of nitrogen 32 passed through this heat exchange device and is mixed with the partial flow of nitrogen 32 passed through the heat exchange device 6 becomes. Instead (not shown), the stream 33 can also be conducted to the warm end of the heat exchange device 6 independently of the partial stream 32. Another nitrogen stream 36 is taken from the upper region of the low-pressure stage 15 and heated in the first heat exchange device 6.

Das Verfahren gemäß Figur 6 ist analog zu demjenigen gemäß Figur 2, allerdings ist hier ebenfalls der zweite Gasstrom ein Stickstoffstrom 32 aus der Druckstufe 7. Die erfindungsgemäße Wärmeübertragung von der zweiten Wärmetauscheinrichtung 10 auf die erste Wärmetauscheinrichtung 6 erfolgt durch indirekten Wärmetausch.in einem Wärmetauscher 25. An einer Zwischenstelle der zweiten Wärmetauscheinrichtung wird ein Teilstrom 34 des verdichteten Stickstoffes 33 abgezweigt, im Wärmetauscher 25 abgekühlt und mit dem am kalten Ende der Wärmetauscheinrichtung 10 austretenden Rest des Stickstoffes 33 vermischt. Stattdessen kann (nicht dargestellt) der Teilstrom 34 auch unabhängig von dem Rest des Stickstoffes 33 entspannt und in die Druckstufe 7 geleitet werden. Von dem in der Wärmetauscheinrichtung 6 anzuwärmenden Teil des Stickstoffes 33 wird ein Teil 35 abgezweigt, der im Wärmetauscher 25 Wärme von dem Teilstrom 34 aufnimmt und anschließend den durch die Wärmetauscheinrichtung 6 geführten Teil des Stickstoffes 33 an einer Zwischenstelle zugeführt wird. Der Teilstrom 35 kann stattdessen (nicht dargestellt) separat zum warmen Ende der Wärmetauscheinrichtung 6 geführt werden.The method according to FIG. 6 is analogous to that according to FIG. 2, but here, too, the second gas stream is a nitrogen stream 32 from the pressure stage 7. The heat transfer according to the invention from the second heat exchange device 10 to the first heat exchange device 6 takes place by indirect heat exchange in a heat exchanger 25 At an intermediate point of the second heat exchange device, a partial flow 34 of the compressed nitrogen 33 is branched off, cooled in the heat exchanger 25 and mixed with the rest of the nitrogen 33 emerging at the cold end of the heat exchange device 10. Instead, can (not shown), the partial flow 34 is also expanded independently of the rest of the nitrogen 33 and passed to the pressure stage 7. From the part of the nitrogen 33 to be heated in the heat exchanger 6, a part 35 is branched off, which absorbs heat from the partial flow 34 in the heat exchanger 25 and then supplies the part of the nitrogen 33 passed through the heat exchanger 6 at an intermediate point. The partial flow 35 can instead (not shown) be conducted separately to the warm end of the heat exchange device 6.

Figur 7 zeigt eine Variante des erfindungsgemäßen Verfahrens, bei der im Unterschied zum Verfahren gemäß Figur 2 der gesamte dritte Teilstrom 12 in der Turbine 14 entspannt wird. Als weiterer Unterschied wird der Stickstoff 17 vom Kopf der Niederdruckstufe 15 nur durch die erste Wärmetauscheinrichtung 6 geführt, wobei wiederum ein Teil des Stickstoffes 17 vor der Wärmetauscheinrichtung 6 abgezweigt und nach Wärmeaufnahme im Wärmetauscher 25 an einer Zwischenstelle der Wärmetauscheinrichtung 6 zugeführt und zusammen mit dem Rest des Stickstoffes 17 weiter angewärmt wird. Der Strom 27 kann (nicht dargestellt) auch separat vom Stickstoff 17 zum warmen Ende der Wärmetauscheinrichtung 6 geführt werden.FIG. 7 shows a variant of the method according to the invention, in which, in contrast to the method according to FIG. 2, the entire third partial stream 12 is expanded in the turbine 14. As a further difference, the nitrogen 17 is led from the head of the low-pressure stage 15 only through the first heat exchange device 6, part of the nitrogen 17 being branched off in front of the heat exchange device 6 and fed to the heat exchange device 6 at an intermediate point after heat absorption in the heat exchanger 25 and together with the rest of nitrogen 17 is further heated. The stream 27 can (not shown) also be conducted separately from the nitrogen 17 to the warm end of the heat exchange device 6.

Das Verfahren gemäß Figur 8 unterscheidet sich von demjenigen gemäß Figur 7 lediglich dadurch, daß der zweite Gasstrom Stickstoff 32 aus der Druckstufe 7 ist. Außerdem erfolgt die Verdichtung des zweiten Gasstroms in zwei Verdichterstufen 9a und 9b.The method according to FIG. 8 differs from that according to FIG. 7 only in that the second gas stream is nitrogen 32 from pressure stage 7. In addition, the second gas stream is compressed in two compressor stages 9a and 9b.

Gemäß Figur 9 wird Luft 101 in einem Luft-Hauptkompressor 102 auf ca. 6 bar verdichtet, in einem Sprühzonenkühler 103 abgekühlt und in umschaltbaren Molekularsiebadsorbern 104 von C02 und H20 befreit. Die gereinigte Luft wird anschließend in zwei Luftströme 105, 106 aufgeteilt. Der mengenmäßig größere Luftstrom 105 wird in einer ersten Wärmetauscheinrichtung 107 in Wärmetausch mit Stickstoff 119, 120 aus der Rektifikation abgekühlt und in die Druckstufe 108 einer zweistufigen Rektifiziersäule eingeleitet. Der zweite Luftstrom 106 wird in zwei Verdichtern 109, 110, auf einen höheren Druck verdichtet (ca. 75 bar) und in einer zweiten Wärmetauscheinrichtung 111 in Wärmetausch mit Stickstoff und Sauerstoff aus der Rektifikation abgekühlt, anschließend in einer Turbine 112 arbeitsleistend auf den Druck der Druckstufe 108 entspannt (ca. 5,9 bar), wobei z.B. über 90% Flüssigkeit anfallen, und in die Druckstufe 108 eingeleitet. Aus der Niederdruckstufe 113 der Rektifiziersäule wird Sauerstoff mit einer Reinheit von beispielsweise 99,5% flüssig entnommen (Leitung 114), mittels einer Pumpe 137 auf den gewünschten Abgabedruck gepumpt und in der Wärmetauscheinrichtung 111 verdampft und angewärmt. Der Abgabedruck in dem gezeigten Beispiel beträgt ca. 70 bar.According to Figure 9 air 101 is in a main air compressor 102 is compressed to about 6 bar, cooled in an Sprühzonenkühler 103 and 104 in the switchable Molekularsiebadsorbern of C02 H20 and freed. The cleaned air is then divided into two air flows 105, 106. The larger airflow 105 is cooled in a first heat exchange device 107 in heat exchange with nitrogen 119, 120 from the rectification and introduced into the pressure stage 108 of a two-stage rectification column. The second air stream 106 is compressed to a higher pressure (approx. 75 bar) in two compressors 109, 110 and cooled in a second heat exchange device 111 in heat exchange with nitrogen and oxygen from the rectification, then in a turbine 112 to perform the pressure of the Pressure stage 108 relaxes (approx. 5.9 bar), for example with more than 90% liquid, and is introduced into pressure stage 108. Oxygen with a purity of, for example, 99.5% liquid is withdrawn from the low-pressure stage 113 of the rectification column (line 114), pumped to the desired delivery pressure by means of a pump 137 and evaporated and heated in the heat exchange device 111. The discharge pressure in the example shown is approx. 70 bar.

Die beiden Stufen der Rektifiziersäule sind durch Verbindungsleitungen 115, 116 miteinander verbunden, Stickstoff 119 vom Kopf der Niederdruckstufe wird in Wärmetauschern 117,118 in Wärmetausch mit den Vorzerlegungsprodukten 115, 116 angewärmt, wobei diese gleichzeitig unterkühlt werden. Der Stickstoff 119 wird je zum Teil durch die beiden Wärmetauscheinrichtungen 107, 111 geführt und angewärmt. Stickstoff 120 vom Kopf der Druckstufe 108 wird in der Wärmetauscheinrichtung 107 angewärmt.The two stages of the rectification column are connected to one another by connecting lines 115, 116, nitrogen 119 from the top of the low-pressure stage is heated in heat exchangers 117, 118 in heat exchange with the pre-separation products 115, 116, these being simultaneously supercooled. The nitrogen 119 is partly passed through the two heat exchangers 107, 111 and heated. Nitrogen 120 from the top of the pressure stage 108 is heated in the heat exchange device 107.

Erfindungsgemäß wird der zweite Luftstrom 106 in zwei Teilströme 121, 122 unterschiedlichen Druckes aufgeteilt. Der erste Teilstrom 122 ist der bereits erwähnte, im Verdichter 110 verdichtete Luftstrom. Der zweite Teilstrom 121 wird durch einen Luftstrom gebildet, der zwischen den beiden Verdichtern 109, 110 abgezweigt wird. Der Luftstrom 121 wird in einem Verdichter 123 von etwa 25 bar auf einen niedrigeren Druck als der im Verdichter 110 verdichtete Luftstrom 122 verdichtet (ca. 33 bar) und in der zweiten Wärmetauscheinrichtung 111 abgekühlt. Bei einer Temperatur, die oberhalb der Entnahmetemperatur des Luftstromes 122 liegt, wird der Luftstrom 121 aus der Wärmetauscheinrichtung 111 entnommen, in einer Turbine 124 arbeitsleistend entspannt und zusammen mit dem Luftstrom 105 in die Druckstufe 108 geleitet. Die Entnahme erfolgt unterhalb der Stelle, an der die geringste Temperaturdifferenz zwischen den kalten und warmen Strömen in der zweiten Wärmetauscheinrichtung 111 herrscht. Die Temperatur am Eingang der Turbine 124 beträgt z.B. 149 K, an der Turbine 112 z.B. 103 K. Die Turbine 124 überträgt ihre Leistung an den Verdichter 123.According to the invention, the second air flow 106 is divided into two partial flows 121, 122 of different pressures. The The first partial flow 122 is the air flow which has already been mentioned and is compressed in the compressor 110. The second partial flow 121 is formed by an air flow which is branched off between the two compressors 109, 110. The air flow 121 is compressed in a compressor 123 from approximately 25 bar to a lower pressure than the air flow 122 compressed in the compressor 110 (approx. 33 bar) and cooled in the second heat exchange device 111. At a temperature which is above the removal temperature of the air flow 122, the air flow 121 is removed from the heat exchange device 111, expanded in a turbine 124 to perform work and passed together with the air flow 105 into the pressure stage 108. The removal takes place below the point at which the smallest temperature difference between the cold and warm flows prevails in the second heat exchange device 111. The temperature at the inlet of the turbine 124 is, for example, 149 K, at the turbine 112, for example, 103 K. The turbine 124 transfers its power to the compressor 123.

Die Kälteleistung der Turbine 124 deckt ca. 80 bis 90% des Kältebedarfs der Anlage, diejenige der Turbine 112 den Rest.The cooling capacity of the turbine 124 covers approximately 80 to 90% of the cooling requirement of the system, that of the turbine 112 the rest.

Gemäß einem weiteren Erfindungsmerkmal wird ein Teil des Stickstoffes 119 an einer Zwischenstelle aus der Wärmetauscheinrichtung 111 abgezweigt und dem durch die Wärmetauscheinrichtung 107 geführten Stickstoff an einer Zwischenstelle zugeführt (Leitung 125). Mit dieser Maßnahme wird Wärme von der zweiten auf die erste Wärmetauscheinrichtung übertragen.According to a further feature of the invention, part of the nitrogen 119 is branched off from the heat exchange device 111 at an intermediate point and fed to the nitrogen passed through the heat exchange device 107 at an intermediate point (line 125). With this measure, heat is transferred from the second to the first heat exchange device.

Das Verfahren gemäß Figur 10 unterscheidet sich von demjenigen gemäß Figur 9 in der Führung der beiden Luftströme 121 und 122. Für die übrigen, analogen Bauteile wurden, wie auch in den folgenden Figuren, dieselben Bezugszeichen wie in Figur 9 verwendet.The method according to FIG. 10 differs from that according to FIG. 9 in the routing of the two air flows 121 and 122. As in the following figures, the same reference numerals as in FIG. 9 were used for the other, analog components.

Der zweite Luft-Teilstrom, der in dem Verdichter 109 auf etwa 52 bar verdichtet wurde, wird z.T. (Luftstrom 121) bei diesem Druck in der zweiten Wärmetauscheinrichtung 111 abgekühlt, an einer Zwischenstelle daraus entnommen und in einer Turbine 124 arbeitsleistend auf den Druck der Druckstufe 108 entspannt, in die er anschließend zusammen mit dem Luftstrom 105 eingeleitet wird. Der zweite Teilstrom 122 wird in einem Verdichter 110 auf einen höheren Druck (ca. 65 bar) verdichtet und in der zweiten Wärmetauscheinrichtung 111 abgekühlt. An deren kaltem Ende wird der Luftstrom 122 entnommen, in der Turbine 112 auf den Druck der Druckstufe 108 entspannt und in diese eingeleitet. Die Turbine 124 ist mit dem Verdichter 110 gekoppelt. .The second partial air flow, which was compressed to about 52 bar in the compressor 109, is partly (Air flow 121) cooled at this pressure in the second heat exchange device 111, removed from it at an intermediate point and relaxed in a turbine 124 to the pressure of the pressure stage 108, into which it is subsequently introduced together with the air flow 105. The second partial flow 122 is compressed to a higher pressure (approx. 65 bar) in a compressor 110 and cooled in the second heat exchange device 111. At its cold end, the air flow 122 is removed, expanded in the turbine 112 to the pressure of the pressure stage 108 and introduced into it. Turbine 124 is coupled to compressor 110. .

Figur 11 zeigt eine Ausführungsform des erfindungsgemäßen Verfahrens, bei der als zweiter Gasstrom ein Kreislaufgas vorgesehen ist. Als Kreislaufgas wird ein Gasstrom 126 aus der Rektifikation entnommen. In dem dargestellten Beispiel erfolgt die Entnahme im unteren Bereich der Druckstufe 108, d.h. der zweite Gasstrom weist eine Zusammensetzung ähnlich wie Luft auf. Es ist aber prinzipiell auch möglich, beispielsweise eine stickstoffreiches Gas vom oberen Bereich der Druckstufe 108 als Kreislaufgas zu verwenden (gestrichelte Darstellung).FIG. 11 shows an embodiment of the method according to the invention in which a recycle gas is provided as the second gas stream. A gas stream 126 is taken from the rectification as the cycle gas. In the example shown, the removal takes place in the lower region of pressure stage 108, i.e. the second gas stream has a composition similar to air. In principle, however, it is also possible to use, for example, a nitrogen-rich gas from the upper region of the pressure stage 108 as the recycle gas (dashed line).

Das Kreislaufgas 126 wird in der ersten Wärmetauscheinrichtung 107 annähernd auf Umgebungstemperatur angewärmt, in zwei Verdichtern 109, 110 verdichtet, in der zweiten Wärmetauscheinrichtung 111 in Wärmetausch mit verdampfendem Sauerstoff abgekühlt, dann in der Turbine 112 arbeitsleistend entspannt und in die Druckstufe 108 geleitet. Vor dem Verdichter 109 wird ein Teil 127 des zweiten Gasstroms abgezweigt, in einem Verdichter 128 auf einen Druck von etwa 6 bis 10 bar verdichtet und in einem Teil der ersten Wärmetauscheinrichtung 107 abgekühlt. An einer Zwischenstelle wird dieser Gasstrom entnommen, in einer mit dem Verdichter 128 gekoppelten Turbine 129 auf den Druck der Niederdruckstufe 113 entspannt und in diese eingeleitet. Der Gasstrom 127 dient zur Kälteerzeugung.The recycle gas 126 is warmed to approximately ambient temperature in the first heat exchange device 107, compressed in two compressors 109, 110, cooled in heat exchange with evaporating oxygen in the second heat exchange device 111, then expanded in the turbine 112 to perform work and passed into the pressure stage 108. A portion 127 of the second gas stream is branched off upstream of the compressor 109, compressed to a pressure of approximately 6 to 10 bar in a compressor 128 and cooled in a portion of the first heat exchange device 107. At an intermediate point this gas flow is withdrawn, expanded to the pressure of the low-pressure stage 113 in a turbine 129 coupled to the compressor 128 and introduced into the latter. The gas flow 127 is used for cooling.

Ein Teilstrom 121 wird zwischen den beiden Verdichtern 109, 110 abgezweigt, in einem Verdichter 123 nachverdichtet und in einem Teil der zweiten Wärmetauscheinrichtung 111 abgekühlt. An einer Zwischenstelle wird der Teilstrom 121 bei einer über dem kalten Ende der zweiten Wärmetauscheinrichtung 111 herrschenden Temperatur entnommen, in einer Turbine 124, die mit dem Verdichter 123 gekoppelt ist, auf den Druck der Druckstufe entspannt und dem Kreislaufgas 126 zugemischt.A partial flow 121 is branched off between the two compressors 109, 110, post-compressed in a compressor 123 and cooled in part of the second heat exchange device 111. At an intermediate point, the partial flow 121 is removed at a temperature prevailing over the cold end of the second heat exchange device 111, expanded to the pressure of the pressure stage in a turbine 124, which is coupled to the compressor 123, and admixed to the cycle gas 126.

Figur 12 zeigt ein Verfahren ähnlich demjenigen gemäß Figur 9, bei dem die zweite Wärmetauscheinrichtung durch drei getrennte Wärmetauscherblöcke 130, 131, 132 gebildet ist. Als weiterer Unterschied ist die Verbindungsleitung 125 weggefallen.FIG. 12 shows a method similar to that according to FIG. 9, in which the second heat exchange device is formed by three separate heat exchanger blocks 130, 131, 132. As a further difference, the connecting line 125 has been omitted.

Der höher verdichtete Teilstrom 122 wird in dem Wärmetauscherblock 130 in Wärmetausch mit verdampfendem Sauerstoff abgekühlt. Ein Teil 133 des Stroms 122 wird an einer Zwischenstelle des Wärmetauscherblocks 130 entnommen und in dem Wärmetauscherblock 131 in Wärmetausch mit einem Teil des Stickstoffes 119 vom Kopf der Niederdruckstufe 113 abgekühlt, anschließend mit dem Rest des im Wärmetauscherblock 130 abgekühlten Teilstroms 122 zusammen in der Turbine 112 arbeitsleistend entspannt und in die Druckstufe 108 geleitet.The higher compressed partial flow 122 is cooled in the heat exchanger block 130 in heat exchange with evaporating oxygen. A portion 133 of the stream 122 is removed at an intermediate point of the heat exchanger block 130 and cooled in the heat exchanger block 131 in heat exchange with a portion of the nitrogen 119 from the top of the low pressure stage 113, then together with the rest of the partial stream 122 cooled in the heat exchanger block 130 in the turbine 112 relaxed while working and passed to pressure stage 108.

Der zwischen den beiden Verdichtern 109, 110 abgezweigte Teilstrom 121 wird nach seiner Verdichtung im Verdichter 123 in dem Wärmetauscherblock 132 in Wärmetausch mit dem im Wärmetauscherblock 131 vorgewärmten Teilstrom des Stickstoffes 119 abgekühlt, anschließend in der Turbine 124 arbeitsleistend entspannt und in die Druckstufe 108 geleitet. Je nach den Verfahrensbedingungen, insbesondere dem Sauerstoff-Abgabedruck, kann die in der Turbine 124 entspannte Luft stattdessen in die Niederdruckstufe 113 geleitet werden (gestrichelte Darstellung).The partial flow 121 branched off between the two compressors 109, 110 is cooled after it has been compressed in the compressor 123 in the heat exchanger block 132 in heat exchange with the partial flow of the nitrogen 119 preheated in the heat exchanger block 131, then in the turbine 124 relaxed while working and passed to pressure stage 108. Depending on the process conditions, in particular the oxygen delivery pressure, the air expanded in the turbine 124 can instead be directed to the low pressure stage 113 (dashed line).

Die Aufteilung der Wärmetauscheinrichtung 111 in drei getrennte Wärmetauscherblöcke 130, 131, 132 ermöglicht es, die Drücke, Mengen und Temperaturen der Luftströme 121, 122 bei einem vorgegebenen Sauerstoffabgabedruck weitgehend voneinander entkoppelt zu variieren und so die optimalen Arbeitspunkte von Verdichtern und Turbine zu wählen. Insbesondere ist die Eintrittstemperatur an der Turbine 124 unabhängig von der Temperaturdifferenz, die zur Verdampfung des Sauerstoffes aufrechterhalten werden muß, wählbar.The division of the heat exchange device 111 into three separate heat exchanger blocks 130, 131, 132 makes it possible to vary the pressures, amounts and temperatures of the air streams 121, 122 largely decoupled from one another at a predetermined oxygen delivery pressure and thus to select the optimal operating points of the compressors and turbine. In particular, the inlet temperature at the turbine 124 can be selected independently of the temperature difference that must be maintained to evaporate the oxygen.

Figur 12 zeigt darüber hinaus in strichpunktierter Darstellung eine zusätzliche Ausgestaltung des erfindungsgemäßen Verfahrens, bei der ein Teil 134 der komprimierten gereinigten Luft 101 in einem Verdichter 135 nachverdichtet, an einer Zwischenstelle aus der ersten Wärmetauscheinrichtung 107 abgezweigt, in einer Turbine 136 arbeitsleistend entspannt und in die Niederdruckstufe 113 geleitet wird.Figure 12 also shows in dash-dotted lines an additional embodiment of the method according to the invention, in which a part 134 of the compressed purified air 101 is compressed again in a compressor 135, branched off at an intermediate point from the first heat exchange device 107, relaxed in a turbine 136 and into the work Low pressure stage 113 is passed.

Mit dem erfindungsgemäßen Verfahren ist es möglich, den Energieverbrauch bei der Innenverdichtung von Sauerstoff größenordnungsmäßig auf denjenigen bei der Außenverdichtung abzusenken.With the method according to the invention, it is possible to reduce the energy consumption in the internal compression of oxygen by an order of magnitude to that in the external compression.

Claims (26)

1. Verfahren zur Gewinnung von gasförmigem 02 unter erhöhtem Druck durch Tieftemperaturrekatifikation von Luft, bei dem Luft komprimiert, gereinigt und mindestens zum Teil in einer ersten Wärmetauscheinrichtung in Wärmetausch mit Zerlegungsprodukt abgekühlt und in die Rektifikation geleitet wird, während ein zweiter Gasstrom auf einen höheren Druck verdichtet, in einer zweiten Wärmetauscheineinrichtung in Wärmetausch mit Zerlegungsprodukt abgekühlt, entspannt und ebenfalls in die Rektifikation geleitet wird, und bei dem Sauerstoff in flüssiger Form aus der Rektifikation entnommen, auf den gewünschten Druck gepumpt und in Wärmetausch mit dem auf höheren Druck verdichteten Gasstrom verdampft und angewärmt wird, dadurch gekennzeichnet, daß ein dritter Teilstrom des zu zerlegenden Gases in Wärmetausch mit Zerlegungsprodukt abgekühlt wird.1. A process for the recovery of gaseous 0 2 under increased pressure by low-temperature recatification of air, in which air is compressed, cleaned and at least partially cooled in a first heat exchange device in heat exchange with decomposition product and passed into the rectification, while a second gas stream to a higher one Compressed pressure, cooled in a second heat exchange device in heat exchange with the decomposition product, expanded and also passed into the rectification, and in which liquid oxygen is removed from the rectification, pumped to the desired pressure and evaporated in heat exchange with the gas stream compressed to higher pressure and is heated, characterized in that a third partial stream of the gas to be decomposed is cooled in heat exchange with the decomposition product. 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als dritter Gasstrom (12) ein Teil der komprimierten gereinigten Luft (1) in der ersten Wärmetauscheinrichtung (6) abgekühlt, mindestens zum Teil an einer Zwischenstelle daraus entnommen und arbeitsleistend entspannt (14) wird, und daß von einer Zwischenstelle der zweiten Wärmetauscheinrichtung (10) Wärme auf eine Zwischenstelle der ersten Wärmetauscheinrichtung (6) übertragen wird.2. The method according to claim 1, characterized in that as a third gas stream (12), a part of the compressed purified air (1) in the first heat exchange device (6) is cooled, at least partially removed therefrom at an intermediate point and relaxed to perform work (14) , and that heat is transferred from an intermediate point of the second heat exchange device (10) to an intermediate point of the first heat exchange device (6). 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß der dritte Gasstrom (12) vor seiner Abkühlung weiterverdichtet (13) wird.3. The method according to claim 1 or 2, characterized in that the third gas stream (12) before it cools further is compressed (13). 4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der dritte Gasstrom (12) nach seiner Entspannung (14) in die Rektifikation und/oder in abziehenden Stickstoff (17) aus der Rektifikation eingeleitet wird.4. The method according to any one of claims 1 to 3, characterized in that the third gas stream (12) after its relaxation (14) in the rectification and / or in withdrawing nitrogen (17) is introduced from the rectification. 5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß der dritte Gasstrom (12) im wesentlichen an der Stelle aus der ersten Wärmetauscheinrichtung (6) entnommen wird, an der die Wärmezuführung erfolgt.5. The method according to any one of claims 1 to 4, characterized in that the third gas stream (12) is taken substantially at the point from the first heat exchange device (6) at which the heat is applied. 6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß der zweite Teilstrom (8,32) arbeitsleistend entspannt (11) wird.6. The method according to any one of claims 1 to 5, characterized in that the second partial stream (8.32) is relaxed to perform work (11). 7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß zur Wärmeübertragung ein Teil (26,34) des verdichteten zweiten Gasstroms (8) vor Beendigung seiner Abkühlung in Wärmetausch mit einem Teil (27,35) eines in der ersten Wärmetauscheinrichtung (6) anzuwärmenden Gasstroms,(17,32) aus der Rektifikation gekühlt wird.7. The method according to any one of claims 1 to 6, characterized in that for heat transfer a part (26,34) of the compressed second gas stream (8) before completion of its cooling in heat exchange with a part (27,35) of one in the first heat exchange device (6) gas stream to be heated, (17.32) is cooled from the rectification. 8. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß die Verdichtung des zweiten Gasstroms (8) in zwei Stufen (9,a, 9b) erfolgt, wobei zwischen den beiden Stufen ein Teilstrom (28) abgezweigt, in der zweiten Wärmetauscheinrichtung (10) abgekühlt und vor Beendigung des Wärmetausches arbeitsleistend entspannt (29) und der Rektifikation zugeführt wird.8. The method according to any one of claims 1 to 7, characterized in that the compression of the second gas stream (8) takes place in two stages (9, a, 9b), a partial stream (28) branching off between the two stages, in the second Cooled heat exchange device (10) and relaxed before the end of the heat exchange work (29) and supplied to the rectification. 9. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß ein Teil (30) des auf seinen endgültigen Druck verdichteten zweiten Gasstroms (8) vor Beendigung des Wärmetauschers abgezweigt, arbeitsleistend entspannt (31) und der Rektifikation zugeführt wird.9. The method according to any one of claims 1 to 8, characterized in that a part (30) of the second gas stream (8) compressed to its final pressure is branched off before the end of the heat exchanger, is relieved of work (31) and is fed to the rectification. 10. Verfahren nach einem der Ansprüche 1 bis 9, dadurch gekennzeichnet, daß Stickstoff (17) aus der Rektifikation jeweils zum Teil durch die erste und die zweite Wärmetauscheinrichtung geführt und ein Teil (24) des Stickstoffes von einer Zwischenstelle der zweiten Wärmetauscheinrichtung (10) dem Stickstoff an einer Zwischenstelle der ersten Wärmetauscheinrichtung (6) zugeführt wird.10. The method according to any one of claims 1 to 9, characterized in that nitrogen (17) from the rectification in each case partly through the first and the second heat exchange device and part (24) of the nitrogen from an intermediate point of the second heat exchange device (10) the nitrogen is supplied at an intermediate point of the first heat exchange device (6). 11. Verfahren nach einem der Ansprüche 1 bis 10, dadurch gekennzeichnet, daß der zweite Gasstrom ein Teilstrom (8) der zu zerlegenden Luft oder ein Gasstrom (32) aus der Druckstufe (7) ist.11. The method according to any one of claims 1 to 10, characterized in that the second gas stream is a partial stream (8) of the air to be separated or a gas stream (32) from the pressure stage (7). 12. Verfahren nach einem der Ansprüche 1 bis 11, dadurch gekennzeichnet, daß die bei der Entspannung des zweiten und/oder dritten Gasstroms gewonnene Arbeit zu dessen Nachverdichtung verwendet wird.12. The method according to any one of claims 1 to 11, characterized in that the work obtained in the expansion of the second and / or third gas stream is used for its post-compression. 13. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als dritter Teilstrom ein Teil des zweiten Gasstromes verwendet wird, wobei der zweite Gasstrom (106, 126) in zwei Teilströme (121,122) aufgespaltet wird, die getrennt voneinander bei verschiedenen Drücken in der zweiten Wärmetauscheinrichtung (111) abgekühlt werden, und daß der Teilstrom (121) mit dem niedrigeren Druck bei einer höheren Temperatur als der höher verdichtete Teilstrom (122) aus der Wärmetauscheinrichtung (111) entnommen, arbeitsleistend entspannt (124) und zumindest teilweise in die Rektifikation geleitet wird.13. The method according to claim 1, characterized in that a part of the second gas stream is used as the third partial stream, the second gas stream (106, 126) being split into two partial streams (121, 122) which are separated from one another at different pressures in the second heat exchange device (111) are cooled, and that the partial flow (121) with the lower pressure at a higher temperature than the higher compressed partial flow (122) is removed from the heat exchange device (111), expanded to perform work (124) and is at least partially passed into the rectification . 14. Verfahren nach Anspruch 13, dadurch gekennzeichnet, daß der auf höheren Druck befindliche Teilstrom (122) nach seiner Abkühlung arbeitsleistend entspannt (112) wird.14. The method according to claim 13, characterized in that the partial flow (122) located at higher pressure is relaxed after its cooling work (112). 15. Verfahren nach Anspruch 13 oder 14, dadurch gekennzeichnet, daß der Teilstrom (121) mit dem niedrigen Druck nach Austritt aus der ersten Verdichterstufe (109) vor seiner Abkühlung nachverdichtet wird.15. The method according to claim 13 or 14, characterized in that the partial flow (121) with the low pressure after leaving the first compressor stage (109) is post-compressed before it cools. 16. Verfahren nach einem der Ansprüche 13 bis 15, dadurch gekennzeichnet, daß der Druck des Teilstroms (121),mit dem niedrigeren Druck zwischen 10 bar und 60 bar beträgt.16. The method according to any one of claims 13 to 15, characterized in that the pressure of the partial stream (121) with the lower pressure is between 10 bar and 60 bar. 17. Verfahren nach einem der Ansprüche 13 bis 16, dadurch gekennzeichnet, daß der Teilstrom (121) mit dem niedrigeren Druck im Bereich der geringsten Temperaturdifferenz zwischen dem Teilstrom (122) mit dem höheren Druck und dem Sauerstoff (114) aus der zweiten Wärmetauscheinrichtung (111) entnommen wird.17. The method according to any one of claims 13 to 16, characterized in that the partial flow (121) with the lower pressure in the region of the lowest temperature difference between the partial flow (122) with the higher pressure and the oxygen (114) from the second heat exchange device ( 111) is removed. 18. Verfahren nach einem der Ansprüche 13 bis 17, dadurch gekennzeichnet, daß die bei der Entspannung (112,124) eines der beiden oder beider Teilströme (121,122) geleistete Arbeit für eine Nachverdichtunq eines der beiden oder beider Teilströme verwendet wird.18. The method according to any one of claims 13 to 17, characterized in that the work performed during the expansion (112, 124) of one of the two or both sub-streams (121, 122) is used for a recompression of one of the two or both sub-streams. 19. Verfahren nach einem der Ansprüche 13 bis 18, dadurch gekennzeichnet, daß Wärme von einer Zwischenstelle der einen auf eine Zwischenstelle der anderen Wärmetauscheinrichtung übertragen wird.19. The method according to any one of claims 13 to 18, characterized in that heat is transferred from an intermediate point of one to an intermediate point of the other heat exchange device. 20. Verfahren nach einem der Ansprüche 13 bis 19, dadurch gekennzeichnet, daß ein Teil (134) der komprimierten, gereinigten Luft (101) an einer Zwischenstelle der ersten Wärmetauscheinrichtung (107) abgezweigt, arbeitsleistend entspannt und in die Rektifikation geleitet wird.20. The method according to any one of claims 13 to 19, characterized in that a part (134) of the compressed, cleaned air (101) at an intermediate point of the first heat exchange device (107) is branched off, relieved of work and passed into the rectification. 21. Verfahren nach Anspruch 20, dadurch gekennzeichnet, daß der abgezweigte Teil der Luft vor seiner Abkühlung nachverdichtet wird.21. The method according to claim 20, characterized in that the branched part of the air is post-compressed before it cools. 22. Verfahren nach einem der Ansprüche 13 bis 21, dadurch gekennzeichnet, daß der zweite Gasstrom (106) ein Teilstrom der eintretenden Luft ist.22. The method according to any one of claims 13 to 21, characterized in that the second gas stream (106) is a partial stream of the incoming air. 23. Verfahren nach einem der Ansprüche 13 bis 22, dadurch gekennzeichnet, daß der zweite Gasstrom (126) aus der Druckstufe (108) entnommen und vor seiner Aufspaltung angewärmt und verdichtet wird.23. The method according to any one of claims 13 to 22, characterized in that the second gas stream (126) is removed from the pressure stage (108) and is heated and compressed before it is split up. 24. Verfahren nach Anspruch 23, dadurch gekennzeichnet, daß ein Teil (127) des zweiten Gasstroms (126) vor seiner Verdichtung nachverdichtet (128), in einer der Wärmetauscheinrichtungen (107,111) abgekühlt, an einer Zwischenstelle daraus entnommen, arbeitsleistend entspannt (129) und in die Rektifikation geleitet wird.24. The method according to claim 23, characterized in that a part (127) of the second gas stream (126) is further compressed before it is compressed (128), cooled in one of the heat exchange devices (107, 111), removed from it at an intermediate point, relieved of work (129) and is directed to the rectification. 25. Vorrichtung zur Durchführung des Verfahrens nach Anspruch 13 mit einem Luft-Hauptkompressor, einer zweistufigen Rektifiziersäule sowie zwei Wärmetauscheinrichtungen, wobei der Luft-Hauptkompressor über die erste Wärmetauscheinrichtung mit der Druckstufe der Rektifiziersäule verbunden ist, während einer zweiten Gasleitung ein zweiter Verdichter zugeordnet ist, der über die zweite Wärmetauscheinrichtung und eine Entspannungsmaschine mit der Druckstufe verbunden ist, wobei eine Sauerstoff-Entnahmeleitung aus der Niederdruckstufe über eine Pumpe durch die zweite Wärmetauscheinrichtung führt, dadurch gekennzeichnet, daß die zweite Gasleitung (106,126) in zwei Teiläste separate Strömungsquerschnitte der zweiten Wärmetauscheinrichtung (111) mündet, wobei zumindest ein Teilast der zweiten Gasleitung einen weiteren Verdichter (110,123) enthält, während der zweite Teilast an einer Zwischenstelle aus der zweiten Wärmetauscheinrichtung (111) geführt und mit einer Entspannungsmaschine (124) verbunden ist, deren Ausgang mit der Rektifiziersäule in Verbindung steht.25. An apparatus for carrying out the method according to claim 13 with an air main compressor, a two-stage rectification column and two heat exchange devices, the air main compressor being connected to the pressure stage of the rectification column via the first heat exchange device, while a second compressor is assigned to a second gas line, which is connected to the pressure stage via the second heat exchange device and a relaxation machine, an oxygen removal line from the low pressure stage being connected via a pump through the second heat exchange device leads, characterized in that the second gas line (106,126) opens into two branches separate flow cross-sections of the second heat exchange device (111), at least one branch of the second gas line contains a further compressor (110,123), while the second branch at an intermediate point from the second heat exchange device (111) and connected to an expansion machine (124), the output of which is connected to the rectification column. 26. Vorrichtung nach Anspruch 25, dadurch gekennzeichnete daß die zweite Wärmetauscheinrichtung (111) mehrere voneinander getrennte Wärmetauscherblöcke (130,131,132) aufweist, von denen ein Wärmetauscherblock (130) Strömungsquerschnitte für Sauerstoff (114) und den höher verdichteten Teil (122) des zweiten Gasstroms, ein zweiter Wärmetauscherblock (131) Strömungsquerschnitte für einen Teilstrom (133) des höher verdichteten Teils (122) des zweiten Gasstroms und einen Stickstoffstrom (119) aus der Rektifiziersäule, sowie ein dritter Wärmetauscherblock (132) Strömungsquerschnitte für den Stickstoffstrom (119) aus dem zweiten Wärmetauscherblock (131) und den niedriger verdichteten Teil (121) des zweiten Gasstroms enthält.26. The apparatus according to claim 25, characterized in that the second heat exchange device (111) has a plurality of mutually separate heat exchanger blocks (130, 131, 132), of which one heat exchanger block (130) has flow cross sections for oxygen (114) and the higher compressed part (122) of the second gas stream, a second heat exchanger block (131) flow cross sections for a partial flow (133) of the higher compressed part (122) of the second gas flow and a nitrogen flow (119) from the rectification column, and a third heat exchanger block (132) flow cross sections for the nitrogen flow (119) from the second Contains heat exchanger block (131) and the lower compressed part (121) of the second gas stream.
EP83104318A 1982-05-03 1983-05-02 Process and apparatus for obtaining gaseous oxygen at elevated pressure Expired EP0093448B1 (en)

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FR2805339A1 (en) * 2000-02-23 2001-08-24 Kobe Steel Ltd PROCESS FOR THE PRODUCTION OF OXYGEN BY CRYOGENIC RECTIFICATION
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US4555256A (en) 1985-11-26
EP0093448B1 (en) 1986-10-15

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