EP2299221A2 - Procédé et dispositif destinés à la décomposition à basse température d'air - Google Patents

Procédé et dispositif destinés à la décomposition à basse température d'air Download PDF

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Publication number
EP2299221A2
EP2299221A2 EP10009045A EP10009045A EP2299221A2 EP 2299221 A2 EP2299221 A2 EP 2299221A2 EP 10009045 A EP10009045 A EP 10009045A EP 10009045 A EP10009045 A EP 10009045A EP 2299221 A2 EP2299221 A2 EP 2299221A2
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EP
European Patent Office
Prior art keywords
pressure
stream
turbine
flow
heat exchanger
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.)
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Application number
EP10009045A
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German (de)
English (en)
Inventor
Alexander Alekseev
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Linde GmbH
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Linde GmbH
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Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP2299221A2 publication Critical patent/EP2299221A2/fr
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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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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
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    • 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
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    • 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
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    • 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
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    • 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
    • F25J3/04096—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 argon or argon enriched stream
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    • 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
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    • 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
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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.
    • 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
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    • 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
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    • 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
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    • 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
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    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/44—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the invention relates to a method according to the preamble of patent claim 1.
  • Such a process in which a liquid pressurized product stream is vaporized against a heat carrier and finally recovered as a gaseous pressure product, is also referred to as an internal compression process. It is particularly common for the production of pressurized oxygen, but can also be used for the production of pressurized nitrogen or Druckargon. In the case of a supercritical pressure no phase transition takes place in the main heat exchanger in the true sense, the product stream is then "pseudo-evaporated".
  • a high-pressure heat carrier is liquefied (or pseudo-liquefied when it is under supercritical pressure), namely a partial flow of air, which is referred to here as "throttle flow”.
  • the turbine stream is originally used for cooling. In plants with internal compression, however, it has a second function; in fact, it helps the inductor current to vaporize (or pseudo-evaporate) the internally compressed streams (nitrogen, oxygen and / or argon).
  • the average temperature difference in the heat exchanger is smaller, the temperature profile cheaper, the system more efficient. That is, it is always advantageous to cool the turbine flow in the heat exchanger as much as possible. As a rule, this leads to the fact that the stream at the outlet from the turbine is not gaseous, but is even partially liquefied.
  • the lowering of the temperature at the inlet to the turbine is not limitless possible, but given in the commonly used machines by a maximum liquid content of about 6% to a maximum of 10% (design criterion). Higher liquid contents can damage the turbine.
  • z is then limited to, for example, the inlet temperature in an air turbine with 60 bar at the entrance and about 85% efficiency with about 169 K. For an inlet pressure of 20 bar, the lowest possible turbine inlet temperature would be about 125 K. If it were possible to set the turbine inlet temperature lower without violating the turbine design criterion, a more efficient process would result.
  • the invention is therefore based on the object of specifying an energy-efficient method and a corresponding device, which can be realized with comparatively low expenditure on equipment.
  • the turbine stream is no longer withdrawn in the course of cooling from an intermediate point of the main heat exchanger, but further, passed through the main heat exchanger, so that the turbine stream - at subcritical pressures down to about the taut or lower cooled or - at supercritical pressure - pseudo-liquefied. Subsequently, it is relaxed to an optimized in terms of work-relaxing relaxation and the temperature profile in the main heat exchanger intermediate pressure, preferably in a throttle valve, and warmed in the main heat exchanger back to the intermediate temperature, which corresponds to the inlet temperature of the work-expansion and which is as low as possible, but so that the turbine design criterion not hurt. For example, this intermediate temperature is below 169 K for a 60 bar turbine stream or below 125 K for a 20 bar turbine stream.
  • the cooling and (pseudo) liquefaction of the turbine flow in the main heat exchanger, when its pressure is equal to that of the Drosseistroms, can be done together with the throttle flow or separately from this.
  • the intermediate pressure to which the turbine flow is released prior to its work expansion is equal to or higher than p inductor current ⁇ p High-pressure column , That is, for a 60-bar inductor current, the intermediate pressure would be 18 bar or higher, or 10.5 bar or 20-bar inductor current (assuming that the pressure in the high-pressure column is 5.5 bar).
  • the relaxation to the intermediate pressure is preferably carried out in a throttle valve.
  • the work-performing relaxation is carried out in a relaxation machine, which is preferably designed as a turbine.
  • the secondary compressor is driven with external energy, and both the Drosseistrom and the turbine flow are at the cooling in the main heat exchanger under the second pressure.
  • Powered by external energy means that the corresponding compressor is driven not by means of energy generated in the air separation process itself, but for example by means of an electric motor, a steam turbine or a gas turbine.
  • the reboiler is driven by a flattening machine operated by a process stream of the process, in particular by the flattening machine (12) operated with the turbine stream (70), the air compressor being the only one driven by external energy Represents machine for the compression of air.
  • a “single machine” is understood here to mean a single-stage or multistage compressor whose stages are all connected to the same drive, all stages being accommodated in the same housing or connected to the same gear.
  • the "first pressure” is significantly above the highest pressure of the distillation column system, in particular significantly above the operating pressure of the high-pressure column. This pressure difference is for example at least 4 bar and is preferably between 6 and 16 bar.
  • the total air compressed in the air compressor (with the exception of possible smaller portions such as instrument air) is preferably completely divided between the Drosse flow and the turbine flow.
  • the process stream which is used to drive the secondary compressor, instead of the turbine flow, for example, by a third air stream, which is relaxed to the operating pressure of the low pressure column (Lachmann turbine) or by pressurized nitrogen from the distillation column system, in particular from a high pressure or low pressure column are formed.
  • the pressure nitrogen can be almost at ambient temperature when entering the corresponding expansion machine, or it is heated to well above ambient temperature before entering the expansion machine ("hot gas expander").
  • the throttle flow may be at a higher pressure than the turbine flow, that is, the turbine flow is lower than the second pressure when cooling in the main heat exchanger and the throttle flow is lower than the second pressure or higher during cooling in the main heat exchanger as the second pressure is.
  • a second after-compressor is used in the second variant, which is driven by a relaxation machine, which is operated with a process stream of the process.
  • the secondary compressor which leads to the second pressure, is driven by the expansion machine, which is operated with the turbine flow, and process flow, which is used to drive the second after-compressor, is replaced by a third air flow, which is expanded to the operating pressure of the low-pressure column ( Lachmann turbine) or by pressurized nitrogen from the distillation column system, in particular from a high-pressure or low-pressure column are formed.
  • the two drives can be reversed.
  • the booster on at least two stages and can also be powered by external energy.
  • the recompression to the second pressure then takes place in at least a first stage of the secondary compressor; the inductor current downstream of the branch of the Turbine flow is at least in the last stage of the post-compressor after-compressed to a third pressure which is higher than the second pressure.
  • the intermediate pressure is 1.5 to 5 bar below the second pressure, that is, the turbine stream is relaxed by this pressure difference before entering the expansion machine.
  • This relatively small throttling causes virtually no energy loss at the low temperature and still allows the desired reduction in the inlet temperature of the expansion machine.
  • the distillation column system comprises a high pressure column and a low pressure column which are in heat exchange relationship via a main condenser.
  • the main capacitor is designed as a condenser-evaporator.
  • the turbine stream is preferably expanded in the expansion machine to approximately the operating pressure of the high-pressure column and at least partially fed into the high-pressure column.
  • the liquid product stream from the distillation column system can be a liquid oxygen stream, a liquid nitrogen stream and / or a liquid argon stream. If more than one product is internally compressed, it goes without saying that correspondingly many independent devices for increasing the pressure (as a rule pumps or pump pairs) and independent passages through the main heat exchanger must be provided.
  • a second air stream is formed from another part of the purified main air stream and the second air stream is cooled below the first pressure in the main heat exchanger and fed to the distillation column system.
  • This second airflow is also referred to as direct airflow.
  • the main air flow is - apart from a small proportion of optionally used as instrument air - divided exactly on the three parts mentioned here, namely direct air flow, turbine flow and inductor current.
  • the invention relates to a device for cryogenic separation of air according to the patent claim 11.
  • the distillation column system 50 comprises a high-pressure column 14, a low-pressure column 15, and a main condenser 16 formed as a condenser-evaporator through which the two columns are in heat exchange relationship.
  • Atmospheric air is sucked in as the main air flow via line 1 from an air compressor 2, where it is brought to a first pressure which corresponds approximately to the operating pressure of the high-pressure column 14, cooled to approximately ambient temperature in a precooling 3 and fed to an adsorptive air purification 4.
  • a first part of the purified main air stream 5 is recompressed as "first air stream" 6 in a secondary compressor 7 to a second pressure of at least 50 bar, for example about 60 bar.
  • the high-pressure air 8 is supplied to the warm end of a main heat exchanger 9 and cooled in the main heat exchanger and pseudo-liquefied.
  • the pseudo-liquefied air is withdrawn via line 10 from the cold end of the main heat exchanger and then divided into a throttle flow 11 and a turbine stream 17.
  • throttle and turbine flow after the common recompression 7 also together in Main heat exchanger cooled and pseudo-liquefied.
  • the turbine stream 17 could be removed slightly above the cold end of the main heat exchanger 9 - see FIG. 2 .
  • the throttle flow (“JT-Air”) 11 is expanded in a throttle valve 12 to about the operating pressure of the high-pressure column and introduced via line 13 at least partially in the liquid state in the high-pressure column 14.
  • a liquid turbine can also be used.
  • a part 43 of the throttle current can be immediately withdrawn from the high pressure column and fed after cooling in a subcooling countercurrent 31 via line 44 of the low pressure column 15 at an intermediate point.
  • the main heat exchanger it is reheated to an intermediate temperature between 140 and 150 K.
  • the turbine stream is withdrawn via line 70 from the main heat exchanger 9 and fed to a turbine 19, which is braked in the example of a generator 20.
  • the air is working expanded to about the operating pressure of the high pressure column.
  • the expanded turbine stream 21 is introduced into a separator (phase separator) 22, in order to separate any liquid fractions, if necessary.
  • Such liquid portions 23 are fed via line 24 at a suitable location in the low-pressure column 15.
  • the gaseous fraction 25 is introduced via line 26 as gaseous feed air ("feed-air”) into the high-pressure column 14.
  • the remainder of the purified main air stream 5 is passed through the main heat exchanger 9 without pressure-changing measures as direct air flow ("second air flow") 27, 28 and continues to flow via line 26 into the high-pressure column 14.
  • a first version of the embodiment (system without argon recovery - "Systems w / o argon”) flows liquid crude oxygen 29 from the bottom of the high pressure column 14 via line 30, subcooling countercurrent 31 and on via line 32 to an intermediate point of the low pressure column.
  • the gaseous Head nitrogen 33 of the high-pressure column 14 is condensed at least in part 34 in the liquefaction space of the main condenser 16. Another part can be passed via line 35 through the main heat exchanger 9 and finally withdrawn via line 36 as gaseous medium pressure product (PGAN).
  • GPN gaseous medium pressure product
  • the condensed nitrogen 37 from the main condenser 16 is fed to a first part 38 as reflux to the high-pressure column 14.
  • a second part 39 is cooled in the subcooling countercurrent 31 and fed via line 40 of the low pressure column 15 as reflux.
  • a nitrogen enriched stream 41, 42 may be passed from an intermediate point of the high pressure column 14 via the subcooling countercurrent 31 to an intermediate position of the low pressure column 15.
  • a low-pressure oxygen product 45 (GOX) can be taken directly in gaseous form, heated in the main heat exchanger 9 and withdrawn via line 46 as a low-pressure product.
  • LOX liquid form
  • IC-LOX, IC "Internal Compression”
  • it is brought by means of an oxygen pump 48 in the liquid state to the desired elevated pressure (first elevated pressure) and fed via line 49 to the cold end of the main heat exchanger 9.
  • the liquid oxygen stream 49 is vaporized or pseudo-vaporized under the increased pressure and warmed to approximately ambient temperature. He finally leaves the plant via line 51 as the first gaseous print product (HP-GOX).
  • another gaseous oxygen product 53, 54 may be recovered under an intermediate pressure that is intermediate the operating pressure of the low pressure column 15 and the elevated pressure downstream of the pump 48 by branching off downstream of the pump 48, respectively (52) and finally vaporized and warmed separately in the main heat exchanger 9.
  • nitrogen may be supplied to an internal compression.
  • a third part 55 of the condensed nitrogen 37 as the second "liquid product stream" from the main condenser 16 (HP-LIN) in a nitrogen pump 56 is brought to a second elevated pressure which corresponds to the desired product pressure and does not have to be equal to the first elevated pressure ,
  • the high-pressure nitrogen is fed via line 57, 58 to the cold end of the main heat exchanger 9.
  • the liquid or supercritical nitrogen stream 58 is vaporized or pseudo-evaporated under the increased pressure and warmed to approximately ambient temperature. He finally leaves the plant via line 59 as the second gaseous pressure product (HP-GAN).
  • MP-GAN gaseous nitrogen product 61, 62
  • impure nitrogen 63, 64, 65 and impure nitrogen 66, 67, 68 are withdrawn in gaseous form from the low-pressure column 15, heated in the supercooling countercurrent 31 and further in the main heat exchanger 9 and withdrawn as low-pressure products (GAN, UN2).
  • some of the products may also be obtained in liquid form, for example liquid nitrogen (LIN) 69 or a portion of the liquid oxygen (LOX) 47 from the bottom of the low-pressure column 15.
  • the process of the first version of the embodiment may also be operated with only a liquid product stream and a gaseous pressure product (for example, either oxygen or nitrogen), or alternatively any combination of the illustrated fluidly pressurized streams 49, 53, 58 and 61 ,
  • a gaseous pressure product for example, either oxygen or nitrogen
  • the distillation column system of the embodiment includes, in addition to the nitrogen-oxygen separation means, an argon part 100 for recovering liquid pure argon (LAR) 105.
  • the argon part has one or more argon-oxygen separation argon columns and a Pure argon column for argon nitrogen separation, which are operated in the known manner.
  • the lower end of the crude argon column communicates via the lines 101 and 102 with an intermediate region of the low-pressure column 15.
  • the crude liquid oxygen 29 from the high-pressure column 11 is in this case passed via the line 129 ("Systems with Argon") in the argon part and in particular at least partially partially evaporated in the top condenser of the crude argon column (s) (not shown).
  • the at least partially vaporized crude oxygen is fed via line 103 into the low-pressure column 15, the liquid remaining via line 132.
  • From the argon part 100 also a gaseous residual stream (waste) 104 is withdrawn.
  • the liquid pure argon 105 may be internally compressed by bringing it as a third "liquid product stream" in an argon pump 106 to a third elevated pressure equal to the desired product pressure and not equal to the first and / or second elevated pressure.
  • the high pressure argon is fed via line 107 to the cold end of the main heat exchanger 9.
  • the argon stream 107 is vaporized or pseudo-evaporated under the increased pressure and warmed to approximately ambient temperature. He finally leaves via line 108 as the third gaseous print product (HP-GAR) the plant.
  • the main heat exchanger can be executed either integrated or split, the drawings show only the basic function of the exchanger - warm streams are cooled by cold.
  • FIG. 2 corresponds in many parts FIG. 1 , Therefore, the same reference numerals have been used for the process steps and apparatus parts already explained above, and the air compressor, the air purification and the distillation column system are in FIG. 2 not shown.
  • FIG. 1 The main difference too FIG. 1 is the higher discharge pressure of the air compressor ("first pressure"), which in FIG. 2 is significantly above the operating pressure of the high pressure column and in the specific example is 17 bar. For this reason, the direct air flow (27 in FIG. 1 ). Rather, the total air is 8 downstream of the post-compressor 7 at about 22 bar ("second pressure") at 203 to the turbine stream 10 and the throttle flow 11 split. (In FIG. 2 the cooling of turbine and throttle flow could also be carried out together, the division inside the main heat exchanger 9 could be made just before the cold end.)
  • the temperature of the turbine flow 17 before the throttling 18 is in the example 1 K to 50 K above the temperature of the cold end, ie the temperature at which the inductor current 11 leaves the main heat exchanger. (Alternatively, the turbine stream could also - as in FIG. 1 shown - are led to the cold end of the main heat exchanger 9.)
  • FIG. 2 the aftercooler 202 of the post-compressor 7, which also in the method according to FIG. 1 is used, but not shown in the drawing there.
  • the reference numeral 201 indicates the optional cooling of the main air stream 5 upstream of the secondary compressor 7 in the main heat exchanger 9.
  • FIG. 3 differs from FIG. 3 by a second expansion machine 319, the second booster 304 with aftercooler 305.
  • the branching in turbine flow and throttle flow takes place here in warm at 303, wherein the inductor current in the second booster 304 from the second pressure (here, for example, 22 bar) to a third Pressure (here, for example, 25 bar) is recompressed, the aftercooler 302 behind the first booster 7 can be omitted when the pre-cooling 201 of the main air flow is used.
  • the second pressure here, for example, 22 bar
  • a third Pressure here, for example, 25 bar
  • FIG. 4 is different from this FIG. 3 in that the second after-compressor 403, which only compresses the throttle flow, is designed as a cold compressor.
EP10009045A 2009-09-21 2010-08-31 Procédé et dispositif destinés à la décomposition à basse température d'air Withdrawn EP2299221A2 (fr)

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DE102009042410 2009-09-21
DE102009048456A DE102009048456A1 (de) 2009-09-21 2009-10-07 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

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EP2520886A1 (fr) * 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
EP2600090A1 (fr) * 2011-12-01 2013-06-05 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
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