EP2963369A1 - Procede et dispositif cryogeniques de separation d'air - Google Patents

Procede et dispositif cryogeniques de separation d'air Download PDF

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Publication number
EP2963369A1
EP2963369A1 EP15001881.0A EP15001881A EP2963369A1 EP 2963369 A1 EP2963369 A1 EP 2963369A1 EP 15001881 A EP15001881 A EP 15001881A EP 2963369 A1 EP2963369 A1 EP 2963369A1
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EP
European Patent Office
Prior art keywords
air
pressure
air flow
turbine
compressed
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Granted
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EP15001881.0A
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German (de)
English (en)
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EP2963369B1 (fr
Inventor
Dimitri Goloubev
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Linde GmbH
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Linde GmbH
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Priority to PL15001881T priority patent/PL2963369T3/pl
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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
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • F25J3/04375—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
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—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
    • 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
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

Definitions

  • the invention relates to a method for the cryogenic separation of air, in which both at least one liquid product and at least one internally compressed product is obtained, wherein two air turbines are used, driving two booster, one of which is designed as a cold compressor.
  • a procedure is over US 2009078001 A1 known.
  • a “main air compressor” is here understood to mean a multi-stage machine whose stages have a common drive (electric motor, steam turbine or gas turbine) and are arranged in a common housing. It may be formed, for example, by a gear compressor in which the steps are grouped around the transmission housing. This transmission has a large gear which drives several parallel pinion shafts with one or two stages each.
  • the distillation column system of the invention can be used as a two-column system (for example, as a classic Linde double column system), or as a three or more column system. It may in addition to the columns for nitrogen-oxygen separation, further devices for obtaining high purity products and / or other air components, in particular of noble gases, for example, an argon production and / or a krypton-xenon recovery.
  • a high-pressure heat carrier is liquefied (or pseudo-liquefied when it is under supercritical pressure).
  • the heat carrier is often formed by a part of the air, in the present case in particular by the first and the fourth air flow.
  • EP 1139046 A1 EP 1146301 A1 .
  • DE 10213212 A1 DE 10213211 A1 .
  • EP 1357342 A1 or DE 10238282 A1 DE 10302389 A1 .
  • DE 10332863 A1 EP 1544559 A1 .
  • EP 1666824 A1 EP 1672301 A1 .
  • DE 102005028012 A1 .
  • WO 2007033838 A1 WO 2007104449 A1 .
  • EP 1845324 A1 is
  • multiple process parameters such as mass flows or pressures are described which are “smaller” or “greater” in one operating mode than in another operating mode.
  • a parameter is "larger” or “smaller” if the difference between the mean values of the parameter in the different operating modes is more than 2%, in particular more than 5%, in particular more than 10%.
  • the natural pressure losses are usually not included here.
  • pressures are considered “equal” if the pressure difference between the corresponding points is not greater than the natural conduction losses caused by pressure losses in piping, heat exchangers, coolers, adsorbers, etc.
  • the first product stream experiences a pressure loss in the passages of the main heat exchanger; nevertheless, here the discharge pressure of the compressed gas product downstream of the main heat exchanger and the pressure upstream of the main heat exchanger are referred to equally as "the first product pressure".
  • the second pressure of a stream downstream of certain process steps is only “lower” or “higher” than the first pressure upstream of these steps, if the corresponding pressure difference is higher than the natural line losses, ie in particular targeted pressure increase by at least one compressor stage or the pressure reduction by at least one throttle valve and / or at least one expansion machine (expansion turbine) takes place.
  • the "main heat exchanger” serves to cool feed air in indirect heat exchange with reflux streams from the distillation column system. It may be formed from a single or multiple parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • the invention has for its object to provide a method of the type mentioned above and a device that can be driven with greatly varying liquid product content.
  • the "liquid product content” include only streams that leave the air separation plant liquid and introduced, for example, in a liquid tank, but not internally compressed streams, although taken from the distillation column system liquid, but vaporized within the air separation plant or pseudo-evaporated and finally in a gaseous state be led out of the air separation plant.
  • the "first mode of operation” is designed for a particularly high liquid production, in particular for maximum liquid production (total amount of liquid products withdrawn from the air separation plant).
  • the “second operating mode” is designed for a lower proportion of liquid product, which may also be zero, for example (pure gas operation).
  • the total amount of liquid products in the second mode of operation is 0%, or slightly higher, for example, between 50% and 100% of the maximum liquid product amount. (All percentages here and below refer to the molar amount, unless stated otherwise.)
  • the molar amount can be given in Nm 3 / h, for example.
  • a turbine-driven cold compressor is used, which is operated in the first operating mode with a lower load than in the second.
  • turbines it does not appear expedient to operate turbines with a lower throughput in the operation with maximum liquid production since turbines can generally be used to produce the refrigeration for the product liquefaction.
  • turbines can generally be used to produce the refrigeration for the product liquefaction.
  • a “cold compressor” is here understood to mean a compression member in which the gas is supplied to the compression at a temperature which is significantly below the ambient temperature, generally below 250 K, preferably below 200 K.
  • the cold compressor can be driven by an electric motor in the inventive method. In many cases, however, it is favorable to use a turbine-cold compressor combination, as described in claim 2.
  • the amount of air passing through the second turbine as the fifth airflow that drives the cold compressor is less in the first mode of operation than in the second mode of operation. In an extreme example, the turbine-cold compressor combination completely out of operation in the first operating mode, ie the corresponding amount of air equal to zero.
  • the inlet pressure of the second turbine may be approximately equal to the inlet pressure of the first turbine; Preferably, however, the two inlet pressures are different. In particular, the inlet pressure of the second turbine may be lower than that of the first turbine and, for example, equal to the first air pressure.
  • the third air pressure may also be higher in the second operating mode than in the first operating mode.
  • the third air flow in the first turbine is relieved to an outlet pressure equal to the operating pressure of the high pressure column (plus line losses).
  • the outlet pressure of the second turbine can also be equal to the operating pressure of the high pressure column (plus line losses) or lower, for example, the operating pressure of the low pressure column (plus line losses), see claims 5 and 6.
  • the third partial flow is then introduced, for example in the low pressure column.
  • the relaxed partial flows can be introduced partially or completely into the high-pressure column, as explained in the claims 7 and 8.
  • more than one internal compaction product can be produced in processes, including more than two interior compaction products.
  • the different internal compaction products may differ in their chemical composition (for example, oxygen / nitrogen or else oxygen or nitrogen of different purity) or in their pressure or both.
  • the invention also relates to an air separation plant in the form of a device according to claim 10.
  • the inventive device can by Device features are added, which correspond to the features of the dependent method claims.
  • the "means for switching between a first and a second operating mode" are complex control and control devices, which allow in cooperation at least partially automatic switching between the two operating modes, for example, a correspondingly programmed operation control system.
  • Atmospheric air 1 (AIR) is sucked in via a filter 2 from a main air compressor 3 and compressed to a first air pressure of, for example, 22 bar. Downstream of the main air compressor 3, the compressed total air 4 is treated under the first air pressure in a precooling device 5 and subsequently in a cleaning device 6. The purified total air 7 is divided into a first air flow 100 and a second air flow 200.
  • AIR Atmospheric air 1
  • the first air stream 100 is cooled in a main heat exchanger 8 from the hot to the cold end and (pseudo-) liquefied and then expanded in a throttle valve 101 to about the operating pressure of the later described high-pressure column, preferably 5 bar to 7 bar, for example 6 bar is.
  • the expanded first air stream 102 is fed via line 9 to the distillation column system, which has a high-pressure column 10, a main condenser 11, which is designed as a condenser-evaporator, and a low-pressure column 12.
  • the second air stream 200 is recompressed in a first turbine-driven secondary compressor 202c with aftercooler 203 to a second air pressure of, for example, 28 bar.
  • the riachver Noticet second air stream 204 is divided into a third air flow 210 and a fourth air flow 230.
  • the third air flow 210 is supplied to the main heat exchanger 8 at the warm end and removed again at a first intermediate temperature T1. Under this intermediate temperature and the second air pressure of the third air flow of a first turbine 202 t is supplied and there work to relax the operating pressure of the high-pressure column 10, which is 5 bar to 7 bar, for example, 6 bar.
  • the first turbine 202t is mechanically coupled to the first boost compressor 202c.
  • the working expanded third air stream 211 is introduced into a separator (phase separator) 212 and there freed of a small proportion of liquid. It then flows in pure gaseous form via the lines 213 and 13 to the sump of the high-pressure column 10.
  • the turbine inlet pressure here is equal to the second air pressure.
  • the bottom liquid 15 of the high pressure column is cooled in a subcooling countercurrent 16 and fed via line 17 to an argon part 500 which will be explained later. From there it exits in part liquid (line 18) and partly gaseous (line 19) inter low pressure column pressure again and is fed at a suitable location in the low-pressure column 12. (If no argon portion is present, the supercooled bottom liquid is immediately depressurized to low pressure column pressure and introduced into the low pressure column.)
  • the gaseous top nitrogen 23 of the high-pressure column 10 is introduced to a first part 24 in the liquefaction space of the main condenser 11 and there substantially completely liquefied.
  • the liquid nitrogen 25 obtained in the process is fed to a first part 26 as reflux to the high-pressure column 10.
  • a second part 27 is cooled in the subcooling countercurrent 16 and fed via valve 28 and line of the low pressure column 12 at the top. Part of it is removed again in the first operating mode via line 30 and recovered as liquid nitrogen product (LIN) and withdrawn from the air separation plant.
  • gaseous low-pressure nitrogen 31 is removed, heated in the supercooling countercurrent 16 and in the main heat exchanger 8 and withdrawn via line 32 as a gaseous low pressure product (GAN).
  • Gaseous impure nitrogen 33 from the low-pressure column is also warmed in supercooling countercurrent 16 and main heat exchanger 8.
  • the warm impure nitrogen 34 can either be blown off via line 35 into the atmosphere (ATM) or be used via line 36 as a regeneration gas in the cleaning device 6.
  • liquid oxygen is withdrawn via line 37.
  • a first part 38 is optionally supercooled in the supercooling countercurrent 16 and recovered via line 39 as a liquid oxygen product (GOX) and withdrawn from the air separation plant.
  • a second part 40 forms the "first product stream" is brought in a pump 41 to a first product, for example, 37 bar, evaporated under this high pressure in the main heat exchanger 16 and warmed to about ambient temperature.
  • the warm pressure oxygen 42 is released as an oxygen-rich first compressed gas product (GOX IC).
  • Another interior compression product may be recovered from a third portion 43 of the liquid nitrogen 25 from the main condenser 11. This is brought as a "second product stream" in a pump 44 liquid to a second product pressure of, for example, 37 bar. Under this second product pressure, it is vaporized in the main heat exchanger 8 and warmed to about ambient temperature. The warm pressure nitrogen 45 is finally released under the second product pressure as a nitrogen-rich compressed gas product (GAN IC).
  • GAN IC nitrogen-rich compressed gas product
  • a third part 230 of the second air flow 204 forms a "fourth air flow"; this is cooled in the main heat exchanger (8) to a first intermediate temperature (T3), further compressed in a cold compressor (14c) to a third air pressure of, for example, 40 bar and flows through the main heat exchanger up to the cold end under this very high pressure.
  • the cold pseudo-liquefied third part 232 is expanded in a throttle valve 233 to high-pressure column pressure and fed via the lines 234 and 9 of the high-pressure column 10.
  • the cold compressor 14c is driven by a second expansion turbine 14t, in which a third partial flow 301 of the compressed total air flow 7 as a "fifth air flow" is released from the first air pressure to the operating pressure High pressure column 10.
  • the second turbine has an inlet temperature T2.
  • the working expanded fifth air flow 302 is introduced via line 13 into the high-pressure column 10.
  • the two turbine inlet temperatures T1 and T2 may be the same in the invention.
  • the air separation plant also includes an argon part 500 which, as in FIG EP 2447563 A1 described and produces another liquid product in the form of liquid pure argon (LAR), which is withdrawn via line 501.
  • argon part 500 which, as in FIG EP 2447563 A1 described and produces another liquid product in the form of liquid pure argon (LAR), which is withdrawn via line 501.
  • the "first total quantity of liquid products”, which is withdrawn from the air separation plant in a first operating mode, in this exemplary embodiment is composed of the streams 30 (LIN), 39 (LOX) and 501 (LAR).
  • the ratio of the total amount of liquid products (LOX, LIN, LAR) to the amount of oxygen-rich compressed gas product 42 (GOX IC, "first compressed gas product") is between 20 and 30%.
  • the turbine 14t power is less than 20% of the power of the turbine 202t.
  • the plant In a second mode of operation, the plant is run with a lower "second total amount of liquid products” and lower ratio of total liquid products (LOX, LIN, LAR) to the amount of oxygen-rich pressurized gas product 42 (GOX IC, "first pressurized gas product”).
  • the flow rate is reduced in at least one of the lines 30 and 39, preferably in both.
  • the argon production is usually not targeted throttled, since in most cases the maximum argon yield is desired. Also, the amounts and pressures of the internal compression products 42, 45 remain constant.
  • the turbine powers are shifted, the turbine 14t is ramped up, in particular to Voillast and the power of the turbine 202t is reduced.
  • the ratio of turbine 14t / 202t power is less than 30%
  • the total amount of air and the discharge pressure of the compressor are reduced, so that the main air compressor 3 consumes less energy.
  • the internal compression process is improved by increasing the fourth and fifth substream 230, 301 and thus providing more high-pressure air 232.
  • the amount of air through the line 100 is less than or equal to the first operating mode.
  • the described process can also be operated at times in a stationary manner, that is, with constant liquid production.
  • the second turbine 14t can also be designed so that it does not blow into the high-pressure column 10, but rather into the low-pressure column 12; Due to the correspondingly increased pressure ratio, more energy can be made available for the cold compressor.
  • the effect of the invention can be further enhanced by connecting a disconnectable second cold compressor downstream of the cold compressor 14c.
  • the stream from the first cold compressor 14c is passed through a second cold compressor in the second operating mode before it is reintroduced into the main heat exchanger.
  • the second cold compressor is driven by an electric motor.
  • the second cold compressor is switched off and the flow from the first cold compressor 14c flows past the second cold compressor via a bypass line.
EP15001881.0A 2014-07-05 2015-06-25 Procede et dispositif cryogeniques de separation d'air Active EP2963369B1 (fr)

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EP15001881.0A EP2963369B1 (fr) 2014-07-05 2015-06-25 Procede et dispositif cryogeniques de separation d'air
PL15001881T PL2963369T3 (pl) 2014-07-05 2015-06-25 Sposób i urządzenie do niskotemperaturowej separacji powietrza

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EP15001881.0A EP2963369B1 (fr) 2014-07-05 2015-06-25 Procede et dispositif cryogeniques de separation d'air

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EP (1) EP2963369B1 (fr)
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US10794630B2 (en) 2017-08-03 2020-10-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating air by cryogenic distillation
EP4151940A1 (fr) * 2021-09-18 2023-03-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation cryogénique d'air

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EP3762127A4 (fr) * 2018-03-09 2021-11-24 O2 Industries Inc. Systèmes, appareil et procédés pour la séparation de l'oxygène à partir de l'air
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CN113758150A (zh) * 2021-09-18 2021-12-07 乔治洛德方法研究和开发液化空气有限公司 空气的低温分离方法和空气分离装置

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RU2015126802A (ru) 2017-01-13
US20160003535A1 (en) 2016-01-07
US11175091B2 (en) 2021-11-16
TWI663373B (zh) 2019-06-21
RU2698378C2 (ru) 2019-08-26
PL2963369T3 (pl) 2018-10-31
CN105318661A (zh) 2016-02-10
CN105318661B (zh) 2019-08-06
TW201629415A (zh) 2016-08-16
EP2963369B1 (fr) 2018-05-02

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