EP2789958A1 - Procédé de décomposition à basse température de l'air et installation de décomposition de l'air - Google Patents

Procédé de décomposition à basse température de l'air et installation de décomposition de l'air Download PDF

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Publication number
EP2789958A1
EP2789958A1 EP13001857.5A EP13001857A EP2789958A1 EP 2789958 A1 EP2789958 A1 EP 2789958A1 EP 13001857 A EP13001857 A EP 13001857A EP 2789958 A1 EP2789958 A1 EP 2789958A1
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European Patent Office
Prior art keywords
pressure
oxygen
intermediate pressure
column
enriched fraction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP13001857.5A
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German (de)
English (en)
Inventor
Wolfgang Haag
Stefan Lochner
Frank Stumpf-Marquardt
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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
Priority to EP13001857.5A priority Critical patent/EP2789958A1/fr
Publication of EP2789958A1 publication Critical patent/EP2789958A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—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 single pressure main column system only
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • F25J3/04284—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
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen enriched compared to air, e.g. "crude 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
    • 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
    • F25J2240/04—Multiple expansion turbines in parallel
    • 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
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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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the invention relates to a process for the cryogenic separation of air and an air separation plant adapted to carry out such a process.
  • the present application relates in particular to the air separation according to the so-called SPECTRA method, such as, inter alia, in US Pat EP 0 412 793 B2 , of the EP 0 773 417 B1 , of the EP 0 780 648 B1 , of the EP 0 807 792 B1 , of the EP 0 932 004 A2 , of the US 2007/204652 A1 or the DE 10 2007 051 184 A1 disclosed.
  • SPECTRA method such as, inter alia, in US Pat EP 0 412 793 B2 , of the EP 0 773 417 B1 , of the EP 0 780 648 B1 , of the EP 0 807 792 B1 , of the EP 0 932 004 A2 , of the US 2007/204652 A1 or the DE 10 2007 051 184 A1 disclosed.
  • the SPECTRA process cools compressed and pre-cleaned air to a temperature suitable for rectification, usually at or near its dew point. It is thereby partially liquefied. The air is then fed into a rectification column and rectified there. Bottom side of the rectification column oxygen-enriched, liquid fractions, head-side nitrogen-enriched, gaseous fractions can be removed. The degree of enrichment depends on the extraction level.
  • the rectification column is taken off a first and a second oxygen-enriched fraction, expanded to an intermediate pressure and then evaporated in a condenser evaporator, which acts as a top condenser of the rectification column.
  • the evaporative refrigeration is used in the overhead condenser to cool a nitrogen-rich fraction, which is also taken from the rectification column.
  • the vaporized first oxygen-enriched fraction is further depressurized in a recuperation machine (booster turbine), whereby exchange losses can be compensated and optionally for product liquefaction, e.g. for nitrogen liquefaction, needed refrigeration can be generated.
  • the first oxygen-enriched fraction can then be discharged below the outlet pressure of the expansion machine, usually under atmospheric pressure or slightly above it, and used, for example, as regeneration gas for adsorption devices for pre-cleaning the feed air.
  • the vaporized second oxygen-enriched fraction is recompressed, cooled, and fed back to the rectification column.
  • a cold compressor can be used for recompression.
  • the expansion machine and the cold compressor may be mechanically interconnected.
  • the invention therefore has the object of improving processes for the cryogenic separation of air and correspondingly operated air separation plants, in particular those with expansion machines.
  • the present invention is based on a conventional process for the cryogenic separation of air, in which, as explained above, it is compressed, cooled and rectified in at least one rectification column.
  • at least one first oxygen-enriched fraction is taken from the at least one rectification column and released from a column pressure to an intermediate pressure and from the intermediate pressure to a final pressure.
  • the column pressure corresponds to the usual operating pressure of the rectification column, as explained below.
  • the invention it is proposed, at least temporarily, to depressurize the first oxygen-enriched fraction from the intermediate pressure to the final pressure at least two, each coupled to a cold compressor, i.
  • a cold compressor i.
  • relaxation machines may be fully connected in parallel, i. have the same inlet and outlet temperatures and pressures.
  • Such an arrangement can be structurally particularly simple and inexpensive to implement, because a variety of components can be designed identical.
  • Corresponding partial flows can also be distributed, for example, via simple branches to be implemented to the mentioned expansion machines.
  • expansion machine in the context of this application refers to a device by means of which the energy released during a relaxation of a fluid can be converted into a mechanical movement and thus taken from a corresponding system.
  • Known relaxation machines are also known as turboexpanders.
  • a "combined with a cold compressor” relaxation machine can directly drive a corresponding cold compressor.
  • a braking device e.g. an oil brake, be provided.
  • the solution proposed according to the invention reduces the power which has to be removed via each individual expansion machine and possibly has to be “destroyed” in an oil brake. Correspondingly more power is available for the operation of the respective cold compressor, which is also mechanically connected to the expansion machine available.
  • the at least two expansion machines each coupled with cold compressors, alternately or simultaneously (in parallel). As explained, this is at least temporarily a fully parallel operation with the same inlet and outlet temperatures and pressures appropriate.
  • the at least two expansion machines each coupled with cold compressors are structurally identical, they can be operated completely redundantly, so that maintenance and / or repair of one of the two machines can be carried out while the other is in regular operation.
  • at least one of the at least two expansion machines mentioned can, for example, also be switched on only in case of high load. Under normal load, two or more expansion machines can also be operated in partial load operation so that their life is extended.
  • the at least two expansion machines can also be constructed differently, so that operation in a first operating state with a first expansion machine and operation in a second operating state with a second expansion machine can be carried out.
  • a method according to the invention advantageously comprises, as column pressure, a pressure of 6 to 20 bar, for example 9 bar, as intermediate pressure a pressure of 2 to 9 bar, for example 4 bar and / or as final pressure a pressure of 0.5 to 1.5 bar, for example, of 1.3 bar to use.
  • the pressures stated in this application are absolute pressures.
  • the method can be adapted to any requirements. Due to the relaxation of the column pressure to the intermediate pressure released cold can be used advantageously for cooling of corresponding fractions, such as a nitrogen fraction. If the aforementioned first oxygen-rich fraction is expanded to a final pressure of, for example, 1.3 bar, it can be fed into a corresponding adsorption device for purification of the air used without further adjustments. It is there, for example, used for the regeneration of the molecular sieves used.
  • a second oxygen-enriched fraction is withdrawn from the at least one rectification column and expanded from the column pressure to the or a further intermediate pressure and then recompressed to the column pressure.
  • at least two cold compressors are used for recompression, these being the cold compressors respectively coupled to the aforementioned at least two expansion machines.
  • the invention thus also proposes the parallel use of a plurality of devices according to an advantageous embodiment. Also with regard to these cold compressors, the advantages explained above with regard to redundancy and / or partial load behavior result.
  • the energy released during the relaxation can therefore advantageously be used at least partially for recompression.
  • the energy released during the expansion from the intermediate pressure to the final pressure, minus the power taken from the oil brake and from losses, is supplied to the respective cold compressor.
  • a mechanical connection which is provided in each case between the cold compressor and expansion machine, may comprise a braking device, which may be designed, for example, as an oil brake.
  • the performance of the braking device serves to cover the cold balance.
  • oil brakes are usually used.
  • one or more relaxation machines may be provided which may be equipped with another braking device, e.g. a generator, as previously mentioned and explained below, are equipped.
  • At least one further expansion machine is used at least temporarily, which is mechanically coupled to a generator, it is possible to recover further energy, e.g. can be used for cooling or compression.
  • the further expansion machine can be switched on when needed and / or operated permanently.
  • Particularly advantageous is the use of such an arrangement whenever at least temporarily the refrigeration demand can not be covered by one or more oil brakes (per expansion machine).
  • oil brakes per expansion machine
  • At least one condenser evaporator to relax the first and / or the second oxygen-enriched fraction from the column pressure to the intermediate pressure or the intermediate pressure and the further intermediate pressure, as explained.
  • This is designed in particular as a head capacitor.
  • a nitrogen-rich fraction which can also be removed from the rectification column.
  • a corresponding nitrogen-rich fraction can be removed after cooling in the condenser and optionally liquefaction of the air separation plant.
  • An air separation plant is set up to carry out the method explained above.
  • At least one rectification column of the air separation plant can at least be taken from a first oxygen-enriched fraction and expanded from a column pressure to an intermediate pressure and from the intermediate pressure to a final pressure.
  • the air separation plant has at least two expansion machines, which are set up to relax the first oxygen-enriched fraction from the intermediate pressure to the final pressure and are each coupled to a cold compressor.
  • FIG. 1 an air separation plant according to the prior art is shown schematically and designated 100 in total.
  • the air separation plant 100 is designed for the cryogenic separation of air according to the SPECTRA method.
  • the air separation plant 100 has a main heat exchanger 1 and a rectification column 2.
  • the main heat exchanger 1 has a so-called warm end 11 and a so-called cold end 12.
  • the main heat exchanger 1 may also be composed of a plurality of individual heat exchangers or heat exchanger blocks and forms in this case a main heat exchanger complex.
  • the rectification column 2 has a head region 21 and a bottom region 22.
  • compressed and pre-cleaned air A is passed through a valve 101 via lines a and b from the hot end 11 to the cold end 12 through the main heat exchanger 1.
  • the air A is thereby cooled to a temperature suitable for rectification, which is normally at or near its dew point. It is thereby partially liquefied.
  • the air A is then fed into the rectification column 2 and rectified there in the usual way.
  • the feeding of the air A takes place, for example, some practical or theoretical plates above the bottom portion 22.
  • the operating pressure of the rectification column 2 referred to in this application as "column pressure" is 6 to 20 bar, for example 9 bar.
  • these oxygen-enriched, liquid fractions, head-side nitrogen-enriched gaseous fractions can be removed.
  • a nitrogen-enriched fraction can be taken from the rectification column 2 via a line c, a first oxygen-enriched fraction via a line e and a second oxygen-enriched fraction via a line d.
  • the degree of oxygenation depends on the extraction level. As explained, the oxygen-enriched fractions used in the context of this application can also be taken at the same level or together.
  • the oxygen-enriched fractions can be guided at the cold end 12 through the main heat exchanger 1 and supercooled. Subsequently, the fractions can be fed via lines g and f to a condenser evaporator designed as a top condenser 3 and vaporized there. By means of expansion valves 111 and 112, the fractions are previously expanded to an intermediate pressure of 2 to 9 bar, for example 4 bar.
  • the lines e and d can be performed without the detour shown on the main heat exchanger 1 directly into the top condenser 3. Other variants are possible.
  • the rectification column 2 are removed and evaporated. This fraction can then be divided into the first and the second oxygen-enriched fraction.
  • the first oxygen-enriched fraction is fed in gaseous form to the main heat exchanger 1 via a line I, where it is heated to an intermediate temperature.
  • a line m at least part of the first oxygen-enriched fraction can subsequently be fed to a relaxation machine 5, which can be in the form of a turboexpander (booster turbine), where it can be expanded to over 300 mbar above atmospheric pressure, for example.
  • a turboexpander boost turbine
  • a further part of the first oxygen-enriched fraction removed from the main heat exchanger at the intermediate temperature may, if required, be expanded alternatively or additionally via a valve 104.
  • the first oxygen-enriched fraction which has been expanded by means of the expansion machine 5 or the valve 104 is then guided through the main heat exchanger 1 via lines n and o from the cold end 12 to the warm end 11 and heated.
  • a suitably heated fraction B can for example be blown off to the atmosphere and / or, if appropriate after further heating, used as regeneration gas in a cleaning device for the air A.
  • the second oxygen-enriched fraction is supplied via one or more h lines gaseously to a cold compressor 4 and recompressed there to about the said column pressure of the rectification column 2.
  • the second oxygen-enriched fraction is recooled via lines i and k in the main heat exchanger 1 again to approximately the operating temperature of the rectification column 2 and fed to the bottom side via a valve 102 in this.
  • a gaseous portion can also be returned via a line shown in dashed lines and another valve 103 in the cold compressor 4 for pump prevention, this is the so-called Boosterbypass.
  • the expansion machine 5 may be mechanically connected to the cold compressor 4 via a braking device 6.
  • the braking device 6 may be formed, for example, as an oil brake.
  • the nitrogen-enriched gaseous fraction withdrawn in the head region 21 of the rectification column 2 can be led in part via the lines p and q from the cold end 12 to the warm end 11 through the main heat exchanger 1. Via a valve 105, the system 100 can thus be taken from gaseous nitrogen C.
  • Another portion of the nitrogen-enriched fraction can be passed through the top condenser 3 via lines r and s and cooled there with the evaporative cooling resulting from the evaporation of the first and second oxygen-rich fractions. Subsequently, a portion of the liquid cooled stream is fed to a heat exchanger 9 and further cooled in countercurrent to a relaxed over a valve 106 portion thereof. Via a line u and a valve 107 can in this way the plant 100, a liquid nitrogen product D are removed. A relaxed by means of the valve 106 portion can also be supplied to the line n and used as previously explained. Via a line t, part of the fraction cooled in the top condenser 3 can be fed back into the head region 21 of the separating column 2.
  • valve 108 and a conduit v may be provided, over which non-supercooled liquid nitrogen may be withdrawn as product from the system. Via a line w and a valve 109 can be blown off into a gaseous flushing fraction F from the line h to the atmosphere.
  • the line x can be used for feeding liquid nitrogen G via a valve 110. Further valves 111 and 112 serve to reduce the pressure of the fluid flows in the respective lines f and g.
  • FIG. 2 an air separation plant according to a particularly preferred embodiment of the invention is shown schematically and designated 10 in total.
  • the air separation plant 10 has the components of the air separation plant 100.
  • two cold compressors 4 instead of only one cold compressor 4 and only one relaxation machine 5 coupled thereto and only one respective braking device 6, two cold compressors 4, two expansion machines 5 and two brake devices 6 are provided according to the embodiment of the invention.
  • the two cold compressors 4 and the two expansion machines 5 are coupled as shown. Also several corresponding units can be provided. These may be structurally identical or deviating from each other.
  • the expansion machines 5 Via the line m or corresponding branches, the expansion machines 5 can be supplied with the same or differently adjustable streams of the second oxygen-enriched fraction removed from the main heat exchanger 1 at the intermediate temperature. The same applies to the first oxygen-rich fraction fed via the line h and the cold compressors 4.
  • a further improvement results when providing a further expansion machine 7, which can be supplied via the line m, a further part of the extracted at the intermediate temperature of the main heat exchanger second oxygen-enriched fraction.
  • the further expansion machine 7 may be mechanically coupled to a generator 8, for example.
  • About the generator 8 can be recovered here in the relaxation released power.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP13001857.5A 2013-04-10 2013-04-10 Procédé de décomposition à basse température de l'air et installation de décomposition de l'air Withdrawn EP2789958A1 (fr)

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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE202018006161U1 (de) 2018-10-23 2019-05-27 Linde Aktiengesellschaft Anlage zur Tieftemperaturzerlegung von Luft
EP3640571A1 (fr) 2018-10-18 2020-04-22 Linde Aktiengesellschaft Procédé et installation de production d'un produit de l'air riche en oxygène
WO2020083525A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2020083528A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2020083527A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2020244801A1 (fr) 2019-06-04 2020-12-10 Linde Gmbh Procédé et installation de décomposition d'air à basse température
EP3772627A1 (fr) 2019-08-09 2021-02-10 Linde GmbH Procédé et installation de séparation d'air à basse température
WO2021078405A1 (fr) 2019-10-23 2021-04-29 Linde Gmbh Procédé et système pour la séparation d'air à basse température
WO2021104668A1 (fr) 2019-11-26 2021-06-03 Linde Gmbh Procédé et installation pour fractionnement à basse température de l'air
WO2021180362A1 (fr) 2020-03-10 2021-09-16 Linde Gmbh Procédé de séparation cryogénique d'air et unité de séparation d'air
WO2021190784A1 (fr) 2020-03-23 2021-09-30 Linde Gmbh Procédé et installation de séparation d'air à basse température
WO2022214214A1 (fr) 2021-04-09 2022-10-13 Linde Gmbh Procédé et installation de fractionnement à basse température d'air
WO2023274574A1 (fr) 2021-07-02 2023-01-05 Linde Gmbh Procédé et installation permettant de fournir un produit à base d'azote, un produit à base d'oxygène et un produit à base d'hydrogène
EP4144432A1 (fr) 2021-09-07 2023-03-08 Linde GmbH Module distributeur pour une installation technique
EP4184100A1 (fr) 2021-11-18 2023-05-24 Linde GmbH Procédé et agencement de production cryogénique pour la production d'un produit d'azote liquide

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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3640571A1 (fr) 2018-10-18 2020-04-22 Linde Aktiengesellschaft Procédé et installation de production d'un produit de l'air riche en oxygène
DE202018006161U1 (de) 2018-10-23 2019-05-27 Linde Aktiengesellschaft Anlage zur Tieftemperaturzerlegung von Luft
WO2020083525A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2020083528A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2020083527A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2020244801A1 (fr) 2019-06-04 2020-12-10 Linde Gmbh Procédé et installation de décomposition d'air à basse température
EP3772627A1 (fr) 2019-08-09 2021-02-10 Linde GmbH Procédé et installation de séparation d'air à basse température
WO2021078405A1 (fr) 2019-10-23 2021-04-29 Linde Gmbh Procédé et système pour la séparation d'air à basse température
WO2021104668A1 (fr) 2019-11-26 2021-06-03 Linde Gmbh Procédé et installation pour fractionnement à basse température de l'air
WO2021180362A1 (fr) 2020-03-10 2021-09-16 Linde Gmbh Procédé de séparation cryogénique d'air et unité de séparation d'air
WO2021190784A1 (fr) 2020-03-23 2021-09-30 Linde Gmbh Procédé et installation de séparation d'air à basse température
WO2022214214A1 (fr) 2021-04-09 2022-10-13 Linde Gmbh Procédé et installation de fractionnement à basse température d'air
WO2023274574A1 (fr) 2021-07-02 2023-01-05 Linde Gmbh Procédé et installation permettant de fournir un produit à base d'azote, un produit à base d'oxygène et un produit à base d'hydrogène
EP4144432A1 (fr) 2021-09-07 2023-03-08 Linde GmbH Module distributeur pour une installation technique
WO2023036460A1 (fr) 2021-09-07 2023-03-16 Linde Gmbh Module de distributeur pour une installation de traitement
EP4184100A1 (fr) 2021-11-18 2023-05-24 Linde GmbH Procédé et agencement de production cryogénique pour la production d'un produit d'azote liquide
EP4184101A1 (fr) 2021-11-18 2023-05-24 Linde GmbH Procédé et installation de production cryogénique pour la production d'un produit liquide contenant de l'azote

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