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EP4528192A1 - Procédé et appareil de séparation cryogénique d'air - Google Patents

Procédé et appareil de séparation cryogénique d'air Download PDF

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Publication number
EP4528192A1
EP4528192A1 EP23020437.2A EP23020437A EP4528192A1 EP 4528192 A1 EP4528192 A1 EP 4528192A1 EP 23020437 A EP23020437 A EP 23020437A EP 4528192 A1 EP4528192 A1 EP 4528192A1
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EP
European Patent Office
Prior art keywords
turbine
pressure
air
lachmann
main
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.)
Pending
Application number
EP23020437.2A
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German (de)
English (en)
Inventor
Daniel OTTE
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Linde GmbH
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Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP23020437.2A priority Critical patent/EP4528192A1/fr
Publication of EP4528192A1 publication Critical patent/EP4528192A1/fr
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—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
    • 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
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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
    • F25J3/04151—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
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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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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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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
    • 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
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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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    • 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

Definitions

  • the invention relates to a method and an apparatus for cryogenic air separation.
  • Classical air separation units comprise rectification column systems which can be designed, for example, as two-column systems, especially double-column systems, but also as three- or multi-column systems.
  • rectification columns for the recovery of nitrogen and/or oxygen in liquid and/or gaseous state, i.e. rectification columns for nitrogen-oxygen separation, rectification columns can be provided for the recovery of other air components, in particular of noble gases.
  • the rectification columns of the rectification column systems just mentioned are typically operated in different pressure ranges.
  • Classical double-column systems comprise a so-called pressure column (also referred to as high pressure column, medium pressure column or lower column) and a so-called low-pressure column (upper column).
  • the pressure column is classically operated in a pressure range of 4 to 7 bar, especially at about 5.3 bar, whereas the low-pressure column is operated in a pressure range of typically 1 to 2 bar, especially at about 1.4 bar. In certain cases, higher pressures can also be used in said rectification columns.
  • the pressures given here and below are absolute pressures at the top of the respective columns.
  • main air compressor/booster air compressor For air separation, so-called main air compressor/booster air compressor (MAC-BAC) processes and so-called high air pressure (HAP) processes can be used.
  • Main air compressor/booster air compressor processes are typically considered more conventional while high air pressure processes are increasingly used as alternatives recently.
  • a high air pressure process is used in the context of the present invention.
  • Main air compressor/booster air compressor processes are characterized by the fact that only a part of the total feed air quantity supplied to the rectification column system is compressed to a pressure in a pressure range which is considerably higher than the pressure range in which the pressure column is typically operated. A further part of the feed air quantity is compressed to a pressure in this pressure range only, or at most to a maximum pressure of 1 to 2 bar above this pressure range, and is fed into the pressure column without further expansion.
  • An example of such a process is for example shown in Figure 2 .3A of Häring (see above).
  • the total amount of air supplied to the pressure column in contrast, the total amount of air supplied to the rectification column system as a whole, is compressed to a pressure in a pressure range that is significantly higher than the pressure range at which the pressure column is operated.
  • a pressure range may, for example, be between 8 and 100 bar.
  • the air fed into the pressure column is therefore expanded in a high-pressure process before being fed into pressure column.
  • High-pressure processes have been described at various places and are known from EP 2 980 514 A1 and EP 2 963 367 A1 , for example.
  • main air compressor/booster air compressor processes are typically considered more energy-efficient as compared to high air pressure processes, the latter may, due to the fact that they do not comprise booster air compressors but use a single machine for air compression, allow for constructing air separation units with reduced capital expenses and maintenance costs.
  • the present invention proposes a process for the cryogenic separation of air and a corresponding plant comprising the features of the independent claims.
  • Preferred embodiments of the present invention are the subject of the dependent claims and the description that follows.
  • the method as proposed herein is particularly suitable for producing gaseous oxygen at a pressure from 4 to 10 bar as a main product, wherein the term "main product” is particularly used to express that further air products, besides the main product are, in total, produced in a smaller amount than the main product, and particularly in an amount corresponding to not more than 50%, 25%, or 10% of the main product.
  • main product is particularly used to express that further air products, besides the main product are, in total, produced in a smaller amount than the main product, and particularly in an amount corresponding to not more than 50%, 25%, or 10% of the main product.
  • turbocompressors In air separation processes and plants, multi-stage turbo compressors are used to compress all the air to be separated, such compressors being referred to as “main air compressors” or “main compressors” for short.
  • the mechanical design of turbocompressors is basically known to the skilled person.
  • a turbocompressor the medium to be compressed is pressurized by means of turbine blades or impellers, which are arranged on a turbine wheel or directly on a shaft.
  • a turbocompressor forms a structural unit, but in a multi-stage turbocompressor this can comprise several compressor stages.
  • a compressor stage usually comprises a turbine wheel or a corresponding arrangement of turbine blades. All these compressor stages can be driven by a common shaft. However, it may also be intended to drive the compressor stages in groups with different shafts, wherein the shafts may also be connected to each other via gearboxes to rotate at different speeds.
  • the main air compressor is characterized by the fact that it compresses the entire quantity of air fed into the column system which is separated for the production of air products, i.e. the entire feed air. Accordingly, a “booster air compressor” or “post compressor” can also be provided, in which, however, only a part of the air volume compressed in the main air compressor is brought to an even higher pressure. This can also be a turbocompressor. For the compression of partial air volumes, further turbocompressors are typically provided, also referred to as boosters, but in comparison to the main air compressor or the booster air compressor, such further turbocompressors only compress air to a relatively small extent.
  • a booster air compressor may also be present in a high-pressure air process where it compresses a partial air volume starting from a high pressure provided by the main air compressor.
  • a booster is referred to as being a "warm booster” if it is supplied with an air feed at a temperature typically above 273 K, particularly above 280 K or above 300 K, and up to 350 K.
  • a booster is referred to as being a "cold booster” if it is supplied with an air feed at a temperature typically below 273 K, particularly below 260 K, below 250 K or below 200 K and particularly down to 150 K or less, more specific values used in an embodiment proposed herein being explained below.
  • Air can also be expanded at several points in air separation units, for which purpose expansion machines in the form of turboexpanders can be used.
  • Turboexpanders can also be coupled to and drive turbocompressors.
  • Turboexpanders are also referred to as “expansion turbines", or for short “turbines” or “expanders” hereinbelow, these terms being used synonymously. If one or more turbocompressors are driven without externally supplied energy, i.e. via one or more turboexpanders, the term “turbine booster” or “booster turbine” is also used for such an arrangement.
  • turboexpander or expansion turbine and the turbocompressor or booster are mechanically coupled, wherein the coupling can be such as to result in the same speed, e.g. via a common shaft, or in different speeds, e.g. via an interposed gearbox.
  • a turbine booster or booster turbine may also include further braking means such as oil brakes, electric generators and the like.
  • Lachmann turbines are used since many years to increase the efficiency of air separation plants. For normal gaseous oxygen plants, 20% to 25% of the process air may be passed through one or more Lachmann turbines at almost its dew point and may then be passed into the low-pressure column at a point which may be just below the entrance of the rich liquid. This operation produces an oxygen product of slightly lower purity and saves energy.
  • Lachmann turbine shall generally describe a turbine which expands air from a pressure generated by the main air compressor into the low-pressure column
  • Lachmann air shall refer to air expanded in a Lachmann turbine.
  • air product in the language used herein, shall refer to a fluid in liquid or gaseous state in which a content of at least one air component such as nitrogen, oxygen, or a noble gas of atmospheric air is higher than in atmospheric air.
  • An air product may be an essentially pure air component, "essentially pure” meaning a content of at least 90%, 95% or 99%.
  • Such an air product may be herein be referred to by using the name of the main component ("oxygen", “nitrogen”, etc.) only, even if minor amounts of one or more other components are present therein.
  • a “liquid product” is an air product which is withdrawn from the air separation unit in liquid state and not evaporated therein, other than internally compressed air products which are initially produced in liquid state and thereafter evaporated or which are withdrawn from the column system already in gaseous state ("gas products").
  • a high air pressure process which includes two turbines, i.e. a Lachmann turbine (also referred to as low-pressure or upper column turbine) and a cold booster turbine (also referred to as medium-pressure, lower column turbine, or Claude turbine) may be used.
  • a Lachmann turbine also referred to as low-pressure or upper column turbine
  • a cold booster turbine also referred to as medium-pressure, lower column turbine, or Claude turbine
  • the high air pressure process is having disadvantages regarding power consumption.
  • the process proposed herein overcomes this and may result in the same or better power characteristics than the main air compressor/booster air compressor process, such that the advantages of the high air pressure process do not anymore come with the drawback of lower energy efficiency.
  • the present invention and its embodiments are based on the finding that the feed temperature of the Lachmann air into the low-pressure column shall be as low as possible to gain in efficiency and argon recovery for the rectification.
  • the turbine inlet temperature of the Lachmann turbine shall be as high as possible to have a higher power and refrigeration generation.
  • the Lachmann turbine inlet and outlet temperatures are fixed by the turbine efficiency.
  • the proposed process now allows for decoupling the low-pressure column feed temperature from the inlet and outlet temperatures of the Lachmann turbine.
  • An aspect of the present invention relates to the use of a cold booster in connection with such an arrangement, such a cold booster being particularly driven by the Lachmann turbine or a medium pressure turbine as explained above, and the Lachmann turbine and the medium pressure turbine particularly being the only turbines in the system.
  • a method of cryogenic air separation using an air separation unit comprising a main air compressor, a main heat exchanger, a Lachmann turbine, a medium pressure turbine, a cold booster mechanically coupled to either the medium pressure turbine or Lachmann turbine, and a rectification column system including a pressure column and a low-pressure column
  • a pressure level which is at least 2 bar, for example at least 4 bar, 6 bar, 8 bar or 10 bar and for example up to 100 bar, above an operating pressure level of the pressure column.
  • the present invention therefore, relates to a high air pressure process as described at the outset, and the outlet pressure of the main air compressor is particularly in a range from 6 to 10 bar, for example from 7 to 9 bar or specifically at about 8.5 bar absolute pressure.
  • a first part of the total air quantity is, after the compression in the main air compressor, subjected, as Lachmann air, to a turboexpansion in the Lachmann turbine and is injected into the low-pressure column, as typical for Lachmann processes.
  • a second part of the total air quantity is, after the compression in the main air compressor, cooled in the main heat exchanger, thereafter subjected to a turboexpansion in the medium pressure turbine, and thereafter injected into the rectification column system, while a third part of the total air quantity is, after the compression in the main air compressor, cooled in the main heat exchanger, thereafter subjected to a compression in the cold booster, and therafter injected into the rectification column system.
  • the Lachmann air is subjected to a post-expansion cooling step after its expansion in the Lachmann turbine and before its injection into the low-pressure column. This decouples, as mentioned, the outlet temperature from (and the inlet temperature to) the Lachmann turbine from the feed temperature into the low-pressure column, resulting in the advantages mentioned before and further below.
  • the inlet temperature of the Lachmann turbine can be set higher, leading to higher refrigeration/power generation of the Lachmann turbine.
  • the third part of the total air quantity is delivered to the cold booster at a temperature level of 105 to 130 K, representing the temperature range to which the third part of the total air quantity is cooled, particulary in the main heat exchanger, and an inlet temperature the cold booster is operated.
  • no further air besides the first and second part of the total air quantity is turboexpanded. This represents a difference from methods of the prior art where further turbines are used, particularly to produce large amounts of liquid air products for which additional cold needs to be generated. Such embodiments allow for constructing an air separation unit with less capital and operating expenses.
  • outlet streams of the Lachmann turbine and of the medium pressure turbine are provided in an at at least partly gaseous state.
  • Such streams may comprise, by mass or volume, a proportion of more than 50, 60, 70, 80 or 90% gas, or they may be provided in an essentially or completely gaseous state.
  • a temperature of the first part of the total air quantity i.e., the Lachmann air
  • the temperature may, in this case, or independently from the ranges indicated, be reduced by at least 12 K in certain embodiments. That means that the Lachmann turbine can operate at a higher temperature with higher cold generation.
  • Embodiments of the present invention include that the first part of the total air quantity, i.e., the Lachmann air, is subjected to a pre-expansion cooling step before its expansion in the Lachmann turbine, wherein a temperature of the first part of the total air quantity is reduced to a temperature in a range from 170 to 220 K, e.g. to about 189 K, in the pre-expansion cooling step.
  • a temperature of the first part of the total air quantity is reduced to a temperature in a range from 170 to 220 K, e.g. to about 189 K, in the pre-expansion cooling step.
  • This contributes to a higher inlet temperature than in standard high air pressure processes.
  • the injection of the first part of the total air quantity, i.e., the Lachmann air, into the low-pressure column may be performed at a position at which an operating temperature thereof, i.e. of the low-pressure column, is in a range from 80 to 90 K, e.g. about 84 K, and the injection into the first part of the total air quantity according to embodiments of the present invention does advantageously not introduce excessive heat here.
  • the post-expansion cooling step is performed using the main heat exchanger and/or using a subcooler or the air separation unit. This enables an efficient use of the apparatus installed in an air separation unit.
  • the Lachmann turbine or the medium pressure turbine and the cold booster are mechanically coupled, as mentioned above, as generally known for a in a turbine booster to recover work freed by expansion.
  • the other turbine not coupled in such a way may also be coupled with a booster or an electric generator.
  • the present invention was found particularly suitable to produce gaseous oxygen at a pressure level of 4 to 8 bar and at a purity of 96.0 to 99.9%, e.g. about 99.5%, oxygen content, thus effectively fulfilling the need of certain consumers.
  • the proposed air separation unit comprising a main air compressor, a main heat exchanger, a Lachmann turbine, a cold booster mechanically coupled to a medium pressure turbine, and a rectification column system including a pressure column and a low-pressure column, is configured to compress at least 90% of a total quantity of air supplied to the rectification column system in the main air compressor to a pressure level which is at least 2 bar above an operating pressure level of the pressure column, and to subject a first part of the total air quantity compressed in the main air compressor thereafter, as Lachmann air, to a turboexpansion in the Lachmann turbine and to inject the same into the low-pressure column.
  • the proposed air separation unit is configured to cool a second part of the total air quantity, after the compression in the main air compressor, in the main heat exchanger and to thereafter subject the same to a turboexpansion in the medium pressure turbine, and thereafter to inject it into the rectification column system.
  • the proposed air separation unit is further configured to cool a third part of the total air quantity, after the compression in the main air compressor, in the main heat exchanger, thereafter subject the same to a compression in the cold booster, and thereafter inject it into the rectification column system.
  • the proposed air separation unit is also configured to subject the first part of the total air quantity to a post-expansion cooling step after its expansion in the Lachmann turbine and before its injection into the low-pressure column.
  • Such an apparatus may particularly include a control unit programmed or adapted to control the apparatus accordingly.
  • FIG. 1 schematically illustrates an air separation unit not being part of the invention.
  • the air separation unit shown in Figure 1 is configured to perform a high air pressure process in which a main air compressor 1 in a "warm" part of the air separation unit, which is not illustrated in detail, is configured to compress essentially the whole air processed in the air separation unit and supplied to a rectification column system 10 to a pressure level which is at least 2 bar above an operating pressure level of a pressure column 11 of the rectification column system, forming a feed air stream a.
  • this pressure may be about 8.5 bar absolute pressure.
  • Further components form also part of the warm part, such as a pre-purification unit, but are not illustrated for reasons of conciseness and because they are known to the skilled person.
  • a partial stream b of feed air stream a is cooled in a main heat exchanger 2 and withdrawn therefrom at a temperature of e.g. about 161 K.
  • Partial stream b is expanded in a Lachmann turbine 3, which is coupled to an electric generator G, to a pressure in a range at which a low-pressure column 12 of the rectification column system 10 is operated.
  • the expanded partial stream still referred to with b, is injected into the low-pressure column 12 at a temperature of e.g. about 104 K at an injection position at which an operating temperature of the low-pressure column 12 is about 84 K.
  • a further partial stream c of feed air stream a is also injected into the main heat exchanger 2.
  • a part thereof is, as an air stream d, withdrawn from the main heat exchanger 2 at an intermediate temperature and expanded in a medium pressure turbine 4 which is coupled to a booster 5.
  • This air stream d is, after said expansion, injected into a phase separator 6 in which a liquid phase and a gaseous phase are separated from each other.
  • a liquid stream e withdrawn from phase separator 6 is combined with a liquid stream f from the pressure column 11 cooled in a subcooler 7 and is thereafter injected to into the low-pressure column 12.
  • a gaseous stream g withdrawn from phase separator 6 is injected into the pressure column 11.
  • a further part of partial stream c is, as an air stream h, also withdrawn from the main heat exchanger 2, but at a lower temperature than air stream d, and is further compressed in booster 5, before being in one part recombined with partial stream c and in a further part, as an air stream I, at least partly liquefied in main heat exchanger 2.
  • a yet further partial stream k of feed air stream a is also at least partly liquefied in main heat exchanger 2. Streams I and k are combined and after their combination injected into the pressure column 11.
  • FIG. 1 The further operation of the air separation unit shown in Figure 1 may correspond to known air separation units and is therefore not explained in detail.
  • a pressurized liquid nitrogen stream s, liquid oxygen t, unpressurized liquid nitrogen u, internally compressed oxygen v, internally compressed nitrogen r, and liquid argon x may, among others, be provided.
  • a stream labelled y is indicated to demonstrate its interconnection.
  • Internal compression pumps 8, 9 are provided.
  • FIGS 2 and 3 show temperature-heat content (Q-T) diagrams for a main air compressor/booster air compressor process (the diagram of Figure 2 ) on the one hand and for a standard high air pressure process as shown in Figure 1 (the diagram of Figure 3 ).
  • Q-T temperature-heat content
  • a temperature in K is indicated on the vertical axis and an enthalpy sum in KW is indicated on the horizontal axis.
  • the upper lines indicates the sum curve of the hot stream, the lower line indicates the sum curve of the cold streams.
  • the graph in Figure 3 is, in other words, representing the heat profile for the given high air pressure solution of Figure 1 .
  • the graph in Figure 2 represents the main air compressor/booster air compressor solution. It can be seen that especially in the cold part the high air pressure process is having power disadvantages. This is leading to approximately 150 KW power difference compared to a main air compressor/booster air compressor process.
  • the proposed process now allows for decoupling the low-pressure column feed temperature from the inlet and outlet temperatures of the Lachmann turbine.
  • the solution of embodiments of the present invention includes that, using a cooling step, the inlet temperature of the Lachmann turbine may be set higher, leading to higher refrigeration/power generation of the Lachmann turbine.
  • FIG 4 schematically illustrates an air separation unit 100 according to an embodiment of the present invention. Only those features differing from the non-inventive air separation unit shown in Figure 1 are explained below.
  • a partial stream of feed air stream a which is indicated with b here as well, is cooled in the main heat exchanger 2 and withdrawn therefrom, but in contrast to the air separation unit shown in Figure 1 at a significantly higher temperature, e.g. at a temperature of about 189 K.
  • This cooling step is referred to as pre-expansion cooling step herein.
  • Partial stream b is, like in the air separation unit shown in Figure 1 , expanded in a Lachmann turbine 3, which is coupled to an electric generator G, to a pressure in a range at which a low-pressure column 12 of the rectification column system 10 is operated.
  • the expanded partial stream leaves the Lachmann turbine 3 at a temperature which is also higher than in the air separation unit shown in Figure 1 , e.g. at a temperature of about 122 K.
  • Stream b is then further cooled to a temperature of e.g. 97 K.
  • This cooling step is referred to as post-expansion cooling step herein.
  • This cooling step can be performed, as shown, in the main heat exchanger 2 only, but also (additionally or alternatively) in subcooler 7.
  • Stream b is injected into the low-pressure column 12 at a temperature of e.g. about 104 K at an injection position at which an operating temperature of the low-pressure column 12 is about 84 K. That is, the injection is performed at essentially the same temperature as in the air separation unit shown in Figure 1 , but the inlet and outlet temperatures of the Lachmann turbine 3 are significantly higher, leading to the advantages explained.
  • the Lachmann turbine 3 inlet temperature is at about 161 K and the Lachmann turbine outlet temperature is at about at 104 K.
  • the expanded Lachmann stream b is fed to the low-pressure column 12. As per column temperature profile at about 84 K, stream b is approximately 20 K too warm when injected in this non-inventive solution into the low-pressure column 12, causing transportation of excess heat to the rectification column system 10 and an evaporation of liquid.
  • the Lachmann turbine inlet temperature in a high air pressure process as illustrated for the air separation unit shown in Figure 1 and for a given mean temperature difference (MTD) of e.g. 5 K at the main heat exchanger 2 conventionally cannot further reduced.
  • MTD mean temperature difference
  • the turbine inlet temperature is at 189 K, turbine outlet temperature at 122 K and the cooled stream downstream the main heat exchanger at 97 K.
  • the higher turbine inlet temperature is leading to an increase of refrigeration power by 20%.
  • the low-pressure column feed temperature enhances the argon production by 0.4%. Total power consumption is improved by 1.2%.
  • Figure 6 shows a partial view of an air separation unit which is an alternative embodiment of the air separation unit shown in Figure 4 .
  • the main heat exchanger 2 and certain streams, i.e. streams b, c, d, h and i, as well as the Lachmann turbine 3, the medium pressure turbine 4, the booster 5, and a generator G are shown.
  • the booster 5 is mechanically coupled with the Lachmann turbine 3 instead of the medium pressure turbine, and the medium pressure turbine is coupled with the generator G.

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EP23020437.2A 2023-09-20 2023-09-20 Procédé et appareil de séparation cryogénique d'air Pending EP4528192A1 (fr)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0644388B1 (fr) * 1993-08-23 1998-10-14 The Boc Group, Inc. Séparation cryogénique d'air
DE102010052544A1 (de) * 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2980514A1 (fr) 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air
DE202021002895U1 (de) * 2021-09-07 2022-02-09 Linde GmbH Anlage zur Tieftemperaturzerlegung von Luft
EP3870916B1 (fr) * 2018-10-26 2023-07-12 Linde GmbH Procédé de production d'un produit ou d'une pluralité de produits de l'air et installation de séparation de l'air

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0644388B1 (fr) * 1993-08-23 1998-10-14 The Boc Group, Inc. Séparation cryogénique d'air
DE102010052544A1 (de) * 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2980514A1 (fr) 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air
EP3870916B1 (fr) * 2018-10-26 2023-07-12 Linde GmbH Procédé de production d'un produit ou d'une pluralité de produits de l'air et installation de séparation de l'air
DE202021002895U1 (de) * 2021-09-07 2022-02-09 Linde GmbH Anlage zur Tieftemperaturzerlegung von Luft

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
"Industrial Gases Processing", 2006, WILEY-VCH, article "Cryogenic Rectification"
F.G. KERRY: "Industrial Gas Handbook: Gas Separation and Purification", 2006, CRC PRESS

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