EP2963371A1 - Method and device for creating a pressurised gas product by the cryogenic decomposition of air - Google Patents

Method and device for creating a pressurised gas product by the cryogenic decomposition of air Download PDF

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Publication number
EP2963371A1
EP2963371A1 EP15001884.4A EP15001884A EP2963371A1 EP 2963371 A1 EP2963371 A1 EP 2963371A1 EP 15001884 A EP15001884 A EP 15001884A EP 2963371 A1 EP2963371 A1 EP 2963371A1
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EP
European Patent Office
Prior art keywords
pressure
air
partial flow
heat exchanger
main heat
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP15001884.4A
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German (de)
French (fr)
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EP2963371B1 (en
Inventor
Dimitri Goloubev
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Linde GmbH
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Linde GmbH
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Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP15001884.4A priority Critical patent/EP2963371B1/en
Publication of EP2963371A1 publication Critical patent/EP2963371A1/en
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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
    • F25J3/04406—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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—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
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    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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    • 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
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    • 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
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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
    • F25J3/04006—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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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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
    • F25J3/04163—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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
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    • F25J3/04187—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
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    • 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
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    • 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
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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
    • 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 and apparatus for variable recovery of a compressed gas product by cryogenic separation of air.
  • the distillation column system of such a system can be designed 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 highly pure products and / or other air components, in particular of noble gases have, for example, an argon production and / or a krypton-xenon recovery.
  • condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
  • Each condenser-evaporator has a liquefaction space and an evaporation space, which consist of liquefaction passages or evaporation passages.
  • the condensation (liquefaction) of the first fluid flow is performed, in the evaporation space the evaporation of the second fluid flow.
  • Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • the evaporation space of a condenser-evaporator can be designed as a bath evaporator, falling-film evaporator or forced-flow evaporator.
  • a liquid product placed under pressure is vaporized against a heat transfer medium and finally recovered as an internally compressed compressed gas product.
  • This method is also called internal compression. It serves to obtain gaseous printed product.
  • the product stream is then "pseudo-evaporated".
  • the product stream may be, for example, an oxygen product from the low-pressure column of a two-column system or a nitrogen product from the high-pressure column of a two-column system or from the liquefaction space of a main condenser via which the high-pressure column and low-pressure column are in heat-exchanging connection
  • a high-pressure heat carrier is liquefied (or pseudo-liquefied when it is under supercritical pressure).
  • the heat transfer medium is often formed by part of the air, in the present case by the "second partial flow" of the compressed feed air.
  • 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
  • the invention relates to systems in which the total feed air is compressed to a pressure well above the highest distillation pressure prevailing inside the columns of the distillation column system (this is normally the high pressure column pressure).
  • HAP processes HAP - high air pressure
  • This is the "first pressure”, ie the outlet pressure of the main air compressor (MAC main air compressor), in which the total air is compressed, for example, more than 4 bar, in particular 6 to 16 bar above the highest distillation pressure.
  • the "first pressure” is between 17 and 25 bar.
  • the main air compressor is regularly the only external energy driven machine for compressing air.
  • a “single machine” is understood to mean a single stage or multi-stage compressor whose stages are all connected to the same drive, with all stages in housed in the same housing or connected to the same gear.
  • MAC-BAC processes in which the air in the main air compressor is compressed to a relatively low total air pressure, for example the operating pressure of the high-pressure column (plus line losses). Part of the air from the main air compressor is compressed to a higher pressure in an external energy driven air booster (BAC).
  • BAC external energy driven air booster
  • This higher pressure air component (often called the choke flow) provides the majority of the heat required for (pseudo) evaporation of the internally compressed product in the main heat exchanger. It is depressurised downstream of the main air compressor in a throttle valve or in a liquid turbine (DLE) to the pressure required in the distillation column system.
  • DLE liquid turbine
  • the invention is based on the object to further improve such a method in terms of energy efficiency.
  • One of the two turbine streams or both can be recompressed together with the second partial flow in the first booster to the second pressure, as described in the claims 3 and 4.
  • the third partial flow can remain without recompression; it is then introduced under the first pressure in the second air turbine.
  • the stream at least partially condensed in the evaporation space of the bottom evaporator of the high-pressure column is then preferably fed to the high-pressure column at an intermediate point.
  • FIGS. 1 and 2 illustrated schematically embodiments.
  • atmospheric air is sucked through a filter 1 from a main air compressor 2.
  • the main air compressor has five stages in the example and compresses the total air flow to a "first pressure", for example 19.7 bar.
  • the total air flow 3 downstream of the main air compressor 2 is cooled under the first pressure in a pre-cooling 4.
  • the pre-cooled total air flow 5 is purified in a cleaning device 6, which is formed in particular by a pair of switchable molecular sieve adsorber.
  • the purified total air flow 7 is recompressed to a first part 8 in a hot air compressor 9 with aftercooler 10 to a "second pressure" of for example 24 bar and then into a "first partial flow” 11 (first turbine air flow) and a "second partial flow”.
  • Divided 12 first inductor current).
  • the first substream 11 is cooled in a main heat exchanger 13 to a first intermediate temperature of about 135K.
  • the cooled first partial flow 14 is expanded in a first air turbine 15 from the second pressure to about 5.5 bar to perform work.
  • the first air turbine 15 drives the warm air compressor 9.
  • the work-performing relaxed first partial flow 16 is introduced into a separator (phase separator) 17.
  • the liquid portion 18 is introduced via lines 19 and 20 into the low-pressure column 22 of the distillation column system.
  • the distillation column system comprises a high-pressure column 21, the low-pressure column 22 and a main condenser 23 and a conventional argon production 24 with crude argon column 25 and pure argon column 26.
  • the main condenser 23 is designed as a condenser-evaporator, in the concrete example as a cascade evaporator.
  • the operating pressure at the top of the high pressure column is in the example 5.3 bar, the one at the top of the low pressure column 1.35 bar.
  • the second partial flow 12 of the feed air is cooled in the main heat exchanger 13 to a second intermediate temperature, which is higher than the first intermediate temperature, fed via line 27 to a cold compressor 28 and there recompressed to a "third pressure" of about 35 bar.
  • the recompressed second partial stream 29 is at a third intermediate temperature, which is higher than the second intermediate temperature, again introduced into the main heat exchanger 13 and cooled there to the cold end.
  • the cold second partial stream 30 is expanded in a throttle valve 31 to approximately the operating pressure of the high-pressure column and fed via line 32 to the high-pressure column 21.
  • a part 33 is removed again, cooled in a supercooling countercurrent 34 and fed via the lines 35 and 20 in the low-pressure column 22.
  • a "third substream" 436 of the feed air is introduced under the second pressure into the main heat exchanger 13 and cooled there to a fourth intermediate temperature, which in the example is slightly higher than the first intermediate temperature.
  • the cooled third partial flow 37 is expanded in a second air turbine 38 from the first pressure to perform work.
  • the working power relaxed turbine stream 339 has a pressure which is at least 1 bar, in particular 4 to 10 bar above the operating pressure of the high-pressure column, and a temperature which is at least 10 K, in particular 15 to 40 K above the inlet temperature of the low-pressure nitrogen streams 55, 61 is located at the cold end of the main heat exchanger. This stream is then further cooled in the cold part of the main heat exchanger.
  • the further cooled third partial flow 340 is expanded as a third throttle flow in a throttle valve 341 to about high-pressure column pressure and introduced via line 32 into the high-pressure column.
  • the heat exchange process in the main heat exchanger can be further optimized, in particular in the case of relatively low GAN-IC pressures of for example 7 to 15 bar, in particular about 12 bar.
  • the second air turbine 38 drives the cold compressor 28.
  • the working expanded third partial flow 339 is supplied via line 40 of the high-pressure column 21 at the bottom.
  • a "fourth partial flow” 41 (second throttle flow) flows through the main heat exchanger 13 from the hot to the cold end under the first pressure.
  • the cold fourth partial stream 42 is expanded in a throttle valve 43 to approximately the operating pressure of the high-pressure column and fed via line 32 to the high-pressure column 21.
  • the oxygen-enriched bottom liquid 44 of the high-pressure column 21 is cooled in the subcooling countercurrent 34 and introduced via line 45 into the optional argon recovery 24. Resulting vapor 46 and remaining liquid 47 are fed into the low-pressure column 22.
  • a first part 49 of the top nitrogen 48 of the high-pressure column 21 is completely or substantially completely liquefied in the liquefaction space of the main condenser 23 against liquid oxygen evaporating in the evaporation space from the bottom of the low-pressure column.
  • a first part 51 of the liquid nitrogen 50 produced in the process is introduced as reflux to the high-pressure column 21.
  • a second part 52 is cooled in the subcooling countercurrent 34, fed via line 53 into the low pressure column 22. At least a portion of the liquid low pressure nitrogen 53 serves as reflux in the low pressure column 21; another part 54 can be obtained as liquid nitrogen product (LIN).
  • gaseous impurity nitrogen 61 is withdrawn, warmed in the supercooling countercurrent 34 and in the main heat exchanger 13.
  • the warm impure nitrogen 62 may be vented (63) into the atmosphere (ATM) and / or used as the regeneration gas 64 for the purifier 6.
  • Gaseous nitrogen 55 from the top of the low pressure column 22 is also heated in the subcooling countercurrent 34 and main heat exchanger 13 and withdrawn via line 56 as low pressure nitrogen product (GAN).
  • the lines 67 and 68 connect the low-pressure column 21 with the crude argon column 25 of argon recovery 24th
  • a first portion 70 of the liquid oxygen 69 from the bottom of the low-pressure column 21 is withdrawn as the "first product stream", brought to a "first product pressure” of, for example, 37 bar in an oxygen pump 71 and vaporized under the first product pressure in the main heat exchanger 13 and finally via line 72 as "first compressed gas product” (GOX IC - compressed gas internal oxygen) won.
  • a second portion 73 of the liquid oxygen 69 from the bottom of the low-pressure column 21 is optionally cooled in the subcooling countercurrent 34 and recovered via line 74 as a liquid oxygen product (LOX).
  • LOX liquid oxygen product
  • a third part 75 of the liquid nitrogen 50 from the high-pressure column 21 and the main condenser 23 is also subjected to internal compression by being brought in a nitrogen pump 76 to a second product pressure of 12 bar, for example, under the second product pressure in the main heat exchanger 13 pseudo and finally recovered via line 77 as internally compressed gaseous nitrogen pressure product (GAN IC).
  • GAN IC internally compressed gaseous nitrogen pressure product
  • a second part 78 of the gaseous top nitrogen 48 of the high-pressure column 21 is warmed in the main heat exchanger and recovered via line 79 either as a gaseous medium pressure product or - as shown - used as a sealing gas (seal gas) for one or more of the illustrated process pumps.
  • FIG. 2 differs from FIG. 1 in that the third partial flow 36 of the feed air is introduced under the first pressure into the main heat exchanger 13 and the second turbine 38 thus has a correspondingly lower inlet pressure.
  • the high-pressure column has a sump evaporator 351. This is used in particular when at least temporarily a particularly low liquid production or even pure gas operation is desired.
  • the turbine 38 of the previous embodiments can not be driven with their maximum throughput, because otherwise too much air would have to be driven as a third partial flow through the cold end of the main heat exchanger and the operation of the main heat exchanger would be less efficient.
  • FIG. 3 can now be passed at a particularly low liquid production part 350 of the third partial flow from the turbine 38 on the main heat exchanger.
  • the turbine 38 (and thus the coupled cold compressor) can now be operated at full throughput, without burdening the heat exchange process in the main heat exchanger.
  • the stream 350 is at least partially condensed in the evaporation space of the bottom evaporator 351 and then via line 352 of High-pressure column fed at an intermediate point. He intensifies the distillation in the lower part of the high-pressure column.
  • the stream 350 can also be cooled to the dew state before it is introduced into the bottom evaporator in the main heat exchanger. This can be done in a separate passage, but also by intermediate removal at a suitable location and appropriate Umspeisung.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

Das Verfahren und die Vorrichtung dienen zur Gewinnung eines Druckgasprodukts (72; 73) mittels Tieftemperaturzerlegung von Luft in einem Destillationssäulen-System, das eine Hochdrucksäule (21) und eine Niederdrucksäule (22) aufweist. Die gesamte Einsatzluft wird in einem Hauptluftverdichter (2) auf einen ersten Druck verdichtet, der mindestens 4 bar höher als der Betriebsdruck der Hochdrucksäule (21) ist. Ein erster Teilstrom (8, 11, 14) der im Hauptluftverdichter (2) verdichteten Einsatzluft (7) wird in einem Hauptwärmetauscher (13) auf eine Zwischentemperatur abgekühlt und in einer ersten Luftturbine (15) arbeitsleistend entspannt. Mindestens ein erster Teil des arbeitsleistend entspannten ersten Teilstroms (16) wird in das Destillationssäulen-System eingeleitet (40; 18, 19, 20). Ein zweiter Teilstrom (12, 27, 29, 30) der im Hauptluftverdichter (2) verdichteten Einsatzluft wird in einem ersten Nachverdichter (9), der insbesondere von der ersten Turbine (15) angetrieben wird, auf einen zweiten Druck nachverdichtet, der höher als der erste Druck ist, in dem Hauptwärmetauscher (13) auf eine Zwischentemperatur abgekühlt, in einem zweiten Nachverdichter (28), der als Kaltverdichter betrieben und insbesondere von der zweiten Turbine (38) angetrieben wird, auf einen dritten Druck nachverdichtet, der höher als der zweite Druck ist, in dem Hauptwärmetauscher (13) abgekühlt und anschließend entspannt (31) und in das Destillationssäulen-System eingeleitet (32). Ein dritter Teilstrom (436, 37) der im Hauptluftverdichter (2) verdichteten Einsatzluft (7) wird in dem Hauptwärmetauscher (13) auf eine Zwischentemperatur abgekühlt und in einer zweiten Luftturbine (38) arbeitsleistend entspannt. Mindestens ein erster Teil (339) des arbeitsleistend entspannten dritten Teilstroms wird in das Destillationssäulen-System eingeleitet (340). Ein erster Produktstrom (69; 75) wird flüssig aus dem Destillationssäulen-System entnommen und einer Druckerhöhung (71; 76) auf einen ersten Produktdruck unterworfen. Der erste Produktstrom wird unter dem ersten Produktdruck im Hauptwärmetauscher (13) verdampft oder pseudo-verdampft und angewärmt. Der angewärmte erste Produktstrom (72; 77) wird als erstes Druckgasprodukt (GOX IC; GAN IC) gewonnen. Der dritte Teilstrom (37) wird in der zweiten Luftturbine (38) auf einen Druck entspannt, der mindestens 1 bar höher als der Betriebsdruck der Hochdrucksäule (21) ist. Mindestens ein erster Teil (339) des arbeitsleistend entspannten dritten Teilstroms wird in dem Hauptwärmetauscher (13) weiter abgekühlt, verflüssigt und anschließend entspannt (341) und in das Destillationssäulen-System eingeleitet.The method and apparatus serve to recover a compressed gas product (72; 73) by cryogenic separation of air in a distillation column system having a high pressure column (21) and a low pressure column (22). The total feed air is compressed in a main air compressor (2) to a first pressure which is at least 4 bar higher than the operating pressure of the high-pressure column (21). A first partial flow (8, 11, 14) of the feed air (7) compressed in the main air compressor (2) is cooled to an intermediate temperature in a main heat exchanger (13) and expanded to perform work in a first air turbine (15). At least a first part of the work-performing expanded first partial flow (16) is introduced into the distillation column system (40, 18, 19, 20). A second partial flow (12, 27, 29, 30) of the feed air compressed in the main air compressor (2) is recompressed in a first secondary compressor (9), which is driven in particular by the first turbine (15), to a second pressure which is higher than the first pressure is, in the main heat exchanger (13) cooled to an intermediate temperature, in a second booster (28), which is operated as a cold compressor and in particular by the second turbine (38), after-compressed to a third pressure which is higher than that second pressure is cooled in the main heat exchanger (13) and then expanded (31) and introduced into the distillation column system (32). A third partial flow (436, 37) of the feed air (7) compressed in the main air compressor (2) is cooled in the main heat exchanger (13) to an intermediate temperature and expanded in a second air turbine (38) to perform work. At least a first portion (339) of the work-performing expanded third substream is introduced into the distillation column system (340). A first product stream (69; 75) is withdrawn liquid from the distillation column system and subjected to a pressure increase (71; 76) to a first product pressure. The first product stream is vaporized or pseudo-vaporized and warmed under the first product pressure in the main heat exchanger (13). The warmed first product stream (72; 77) is recovered as the first compressed gas product (GOX IC; GAN IC). The third partial flow (37) is expanded in the second air turbine (38) to a pressure which is at least 1 bar higher than the operating pressure of the high-pressure column (21). At least a first part (339) of the work-performing expanded third partial stream is further cooled in the main heat exchanger (13), liquefied and then expanded (341) and introduced into the distillation column system.

Description

Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur variablen Gewinnung eines Druckgasprodukts mittels Tieftemperaturzerlegung von Luft.The invention relates to a method and apparatus for variable recovery of a compressed gas product by cryogenic separation of air.

Verfahren und Vorrichtungen zur Tieftemperaturzerlegung von Luft sind zum Beispiel aus Hausen/Linde, Tieftemperaturtechnik, 2. Auflage 1985, Kapitel 4 (Seiten 281 bis 337 ) bekannt.For example, methods and apparatus for cryogenic decomposition of air are off Hausen / Linde, Tiefftemperaturtechnik, 2nd edition 1985, chapter 4 (pages 281 to 337 ) known.

Das Destillationssäulen-System einer solchen Anlage kann als Zwei-Säulen-System (zum Beispiel als klassisches Linde-Doppelsäulensystem) ausgebildet sein, oder auch als Drei- oder Mehr-Säulen-System. Es kann zusätzlich zu den Kolonnen zur Stickstoff-Sauerstoff-Trennung weitere Vorrichtungen zur Gewinnung hoch reiner Produkte und/oder anderer Luftkomponenten, insbesondere von Edelgasen aufweisen, beispielsweise eine Argongewinnung und/oder eine Krypton-Xenon-Gewinnung.The distillation column system of such a system can be designed 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 highly pure products and / or other air components, in particular of noble gases have, for example, an argon production and / or a krypton-xenon recovery.

Als "Kondensator-Verdampfer" wird ein Wärmetauscher bezeichnet, in dem ein erster, kondensierender Fluidstrom in indirekten Wärmeaustausch mit einem zweiten, verdampfenden Fluidstrom tritt. Jeder Kondensator-Verdampfer weist einen Verflüssigungsraum und einen Verdampfungsraum auf, die aus Verflüssigungspassagen beziehungsweise Verdampfungspassagen bestehen. In dem Verflüssigungsraum wird die Kondensation (Verflüssigung) des ersten Fluidstroms durchgeführt, in dem Verdampfungsraum die Verdampfung des zweiten Fluidstroms. Verdampfungs- und Verflüssigungsraum werden durch Gruppen von Passagen gebildet, die untereinander in Wärmeaustauschbeziehung stehen. Der Verdampfungsraum eines Kondensator-Verdampfers kann als Badverdampfer, Fallfilmverdampfer oder Forced-Flow-Verdampfer ausgebildet sein.The term "condenser-evaporator" refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream. Each condenser-evaporator has a liquefaction space and an evaporation space, which consist of liquefaction passages or evaporation passages. In the liquefaction space, the condensation (liquefaction) of the first fluid flow is performed, in the evaporation space the evaporation of the second fluid flow. Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other. The evaporation space of a condenser-evaporator can be designed as a bath evaporator, falling-film evaporator or forced-flow evaporator.

Bei dem Prozess der Erfindung wird ein flüssig auf Druck gebrachter Produktstrom gegen einen Wärmeträger verdampft und schließlich als innenverdichtetes Druckgasprodukt gewonnen. Diese Methode wird auch als Innenverdichtung bezeichnet. Sie dient zur Gewinnung von gasförmigem Druckprodukt. Für den Fall eines überkritischen Drucks findet kein Phasenübergang im eigentlichen Sinne statt, der Produktstrom wird dann "pseudo-verdampft". Bei dem Produktstrom kann es sich beispielsweise um ein Sauerstoffprodukt aus der Niederdrucksäule eines Zwei-SäulenSystems oder um ein Stickstoffprodukt aus der Hochdrucksäule eines Zwei-SäulenSystems beziehungsweise aus dem Verflüssigungsraum eines Hauptkondensators handeln, über den Hochdrucksäule und Niederdrucksäule in wärmetauschender Verbindung stehenIn the process of the invention, a liquid product placed under pressure is vaporized against a heat transfer medium and finally recovered as an internally compressed compressed gas product. This method is also called internal compression. It serves to obtain gaseous printed product. In the case a supercritical pressure, no phase transition takes place in the true sense, the product stream is then "pseudo-evaporated". The product stream may be, for example, an oxygen product from the low-pressure column of a two-column system or a nitrogen product from the high-pressure column of a two-column system or from the liquefaction space of a main condenser via which the high-pressure column and low-pressure column are in heat-exchanging connection

Gegen den (pseudo-)verdampfenden Produktstrom wird ein unter hohem Druck stehender Wärmeträger verflüssigt (beziehungsweise pseudo-verflüssigt, wenn er unter überkritischem Druck steht). Der Wärmeträger wird häufig durch einen Teil der Luft gebildet, im vorliegenden Fall von dem "zweiten Teilstrom" der verdichteten Einsatzluft.Against the (pseudo) evaporating product stream, a high-pressure heat carrier is liquefied (or pseudo-liquefied when it is under supercritical pressure). The heat transfer medium is often formed by part of the air, in the present case by the "second partial flow" of the compressed feed air.

Innenverdichtungsverfahren sind zum Beispiel bekannt aus DE 830805 , DE 901542 (= US 2712738 / US 2784572 ), DE 952908 , DE 1103363 (= US 3083544 ), DE 1112997 (= US 3214925 ), DE 1124529 , DE 1117616 (= US 3280574 ), DE 1226616 (= US 3216206 ), DE 1229561 (= US 3222878 ), DE 1199293 , DE 1187248 (= US 3371496 ), DE 1235347 , DE 1258882 (= US 3426543 ), DE 1263037 (= US 3401531 ), DE 1501722 (= US 3416323 ), DE 1501723 (= US 3500651 ), DE 253132 (= US 4279631 ), DE 2646690 , EP 93448 B1 (= US 4555256 ), EP 384483 B1 (= US 5036672 ), EP 505812 B1 (= US 5263328 ), EP 716280 B1 (= US 5644934 ), EP 842385 B1 (= US 5953937 ), EP 758733 B1 (= US 5845517 ), EP 895045 B1 (= US 6038885 ), DE 19803437 A1 , EP 949471 B1 (= US 6185960 B1 ), EP 955509 A1 (= US 6196022 B1 ), EP 1031804 A1 (= US 6314755 ), DE 19909744 A1 , EP 1067345 A1 (= US 6336345 ), EP 1074805 A1 (= US 6332337 ), DE 19954593 A1 , EP 1134525 A1 (= US 6477860 ), DE 10013073 A1 , EP 1139046 A1 , EP 1146301 A1 , EP 1150082 A1 , EP 1213552 A1 , DE 10115258 A1 , EP 1284404 A1 (= US 2003051504 A1 ), EP 1308680 A1 (= US 6612129 B2 ), DE 10213212 A1 , DE 10213211 A1 , EP 1357342 A1 oder DE 10238282 A1 DE 10302389 A1 , DE 10334559 A1 , DE 10334560 A1 , DE 10332863 A1 , EP 1544559 A1 , EP 1585926 A1 , DE 102005029274 A1 EP 1666824 A1 , EP 1672301 A1 , DE 102005028012 A1 , WO 2007033838 A1 , WO 2007104449 A1 , EP 1845324 A1 , DE 102006032731 A1 , EP 1892490 A1 , DE 102007014643 A1 , A1, EP 2015012 A2 , EP 2015013 A2 , EP 2026024 A1 , WO 2009095188 A2 oder DE 102008016355A1 .Internal compression methods are known, for example DE 830805 . DE 901542 (= US 2712738 / US 2784572 ) DE 952908 . DE 1103363 (= US 3,083,544 ) DE 1112997 (= US 3214925 ) DE 1124529 . DE 1117616 (= US 3280574 ) DE 1226616 (= US 3216206 ) DE 1229561 (= US 3222878 ) DE 1199293 . DE 1187248 (= US 3371496 ) DE 1235347 . DE 1258882 (= US 3426543 ) DE 1263037 (= US 3401531 ) DE 1501722 (= US 3,416,323 ) DE 1501723 (= US 3,500,651 ) DE 253132 (= US 4279631 ) DE 2646690 . EP 93448 B1 (= US 4555256 ) EP 384483 B1 (= US 5036672 ) EP 505812 B1 (= US 5263328 ) EP 716280 B1 (= US 5644934 ) EP 842385 B1 (= US 5953937 ) EP 758733 B1 (= US 5845517 ) EP 895045 B1 (= US 6038885 ) DE 19803437 A1 . EP 949471 B1 (= US 6,189,960 B1 ) EP 955509 A1 (= US 6196022 B1 ) EP 1031804 A1 (= US 6314755 ) DE 19909744 A1 . EP 1067345 A1 (= US 6336345 ) EP 1074805 A1 (= US 6332337 ) DE 19954593 A1 . EP 1134525 A1 (= US 6477860 ) DE 10013073 A1 . EP 1139046 A1 . EP 1146301 A1 . EP 1150082 A1 . EP 1213552 A1 . DE 10115258 A1 . EP 1284404 A1 (= US 2003051504 A1 ) EP 1308680 A1 (= US 6612129 B2 ) DE 10213212 A1 . DE 10213211 A1 . EP 1357342 A1 or DE 10238282 A1 DE 10302389 A1 . DE 10334559 A1 . DE 10334560 A1 . DE 10332863 A1 . EP 1544559 A1 . EP 1585926 A1 . DE 102005029274 A1 EP 1666824 A1 . EP 1672301 A1 . DE 102005028012 A1 . WO 2007033838 A1 . WO 2007104449 A1 . EP 1845324 A1 . DE 102006032731 A1 . EP 1892490 A1 . DE 102007014643 A1 , A1, EP 2015012 A2 . EP 2015013 A2 . EP 2026024 A1 . WO 2009095188 A2 or DE 102008016355A1 ,

Die Erfindung betrifft insbesondere Systeme, bei denen die gesamte Einsatzluft auf einen Druck verdichtet wird, der deutlich über dem höchsten Destillationsdruck, der im Inneren der Säulen des Destillationssäulen-Systems herrscht (im Normalfall ist dies der Hochdrucksäulendruck). Solche Systeme werden auch als HAP-Prozesse bezeichnet (HAP - high air pressure). Dabei liegt der "erste Druck", also der Austrittsdruck des Hauptluftverdichters (MAC = main air compressor), in dem die Gesamtluft verdichtet wird, beispielsweise mehr als 4 bar, insbesondere 6 bis 16 bar über dem höchsten Destillationsdruck. Absolut liegt der "erste Druck" beispielsweise zwischen 17 und 25 bar. Bei HAP-Verfahren stellt der Hauptluftverdichter regelmäßig die einzige mit externer Energie angetriebene Maschine zur Verdichtung von Luft dar. Unter einer "einzigen Maschine" wird hier ein einstufiger oder mehrstufiger Verdichter verstanden, dessen Stufen alle mit dem gleichen Antrieb verbunden sind, wobei alle Stufen in demselben Gehäuse untergebracht oder mit demselben Getriebe verbunden sind.More particularly, the invention relates to systems in which the total feed air is compressed to a pressure well above the highest distillation pressure prevailing inside the columns of the distillation column system (this is normally the high pressure column pressure). Such systems are also referred to as HAP processes (HAP - high air pressure). This is the "first pressure", ie the outlet pressure of the main air compressor (MAC = main air compressor), in which the total air is compressed, for example, more than 4 bar, in particular 6 to 16 bar above the highest distillation pressure. In absolute terms, for example, the "first pressure" is between 17 and 25 bar. In HAP processes, the main air compressor is regularly the only external energy driven machine for compressing air. A "single machine" is understood to mean a single stage or multi-stage compressor whose stages are all connected to the same drive, with all stages in housed in the same housing or connected to the same gear.

Eine Alternative zu derartigen HAP-Verfahren stellen so genannte MAC-BAC-Verfahren dar, bei denen die Luft im Hauptluftverdichter auf einen relativ niedrigen Gesamtluftdruck verdichtet wird, zum Beispiel auf den Betriebsdruck der Hochdrucksäule (plus Leitungsverlusten). Ein Teil der Luft aus dem Hauptluftverdichter wird in einem mit externer Energie angetriebenen Luftnachverdichter (BAC = booster air compressor) auf einen höheren Druck verdichtet. Dieser Luftteil unter höherem Druck (häufig Drosselstrom genannt) liefert den Großteil der für die (Pseudo-)Verdampfung des innenverdichteten Produkts notwendige Wärme im Hauptwärmetauscher. Er wird stromabwärts des Hauptluftverdichters in einem Drosselventil oder in einer Flüssigturbine (DLE = dense liquid expander) auf den im Destillationssäulen-System benötigten Druck entspannt.An alternative to such HAP processes are so-called MAC-BAC processes, in which the air in the main air compressor is compressed to a relatively low total air pressure, for example the operating pressure of the high-pressure column (plus line losses). Part of the air from the main air compressor is compressed to a higher pressure in an external energy driven air booster (BAC). This higher pressure air component (often called the choke flow) provides the majority of the heat required for (pseudo) evaporation of the internally compressed product in the main heat exchanger. It is depressurised downstream of the main air compressor in a throttle valve or in a liquid turbine (DLE) to the pressure required in the distillation column system.

Ein Verfahren der eingangs genannten Art mit serielle verbundenem erstem Nachverdichter (Warmbooster) und zweitem Nachverdichter (Kaltbooster) ist aus DE 102010055448 A1 bekannt.A method of the type mentioned with serial connected first booster (warm booster) and second booster (cold booster) is out DE 102010055448 A1 known.

Der Erfindung liegt die Aufgabe zugrunden, ein derartiges Verfahren hinsichtlich der energetischen Effizienz weiter zu verbessern.The invention is based on the object to further improve such a method in terms of energy efficiency.

Diese Aufgabe wird durch die Merkmale des Patentanspruchs 1 gelöst. Neben dem "zweiten Teilstrom" - dem Drosselstrom unter dem besonders hohen dritten Druck - wird ein weiterer Drosselstrom unter einem vergleichsweise niedrigen Druck von beispielsweise 7 bis 15 bar, insbesondere 10 bis 13 bar durch den kalten Teil des Hauptwärmetauschers gefahren. Dieser weitere Drosselstrom wird durch den "dritten Teilstrom" der Luft stromabwärts seiner Entspannung in der zweiten Luftturbine gebildet. Der zusätzliche Luftstrom im kalten Teil des Hauptwärmetauschers ermöglicht es, ein günstiges Wärmetauschdiagramm zu erreichen und damit Energie zu sparen, insbesondere wenn als innenverdichtetes Produkt Stickstoff zwischen 7 und 15 bar gewonnen wird.This object is solved by the features of patent claim 1. In addition to the "second partial flow" - the throttle flow under the particularly high third pressure - another throttle flow is driven at a comparatively low pressure, for example 7 to 15 bar, in particular 10 to 13 bar through the cold part of the main heat exchanger. This further inductor current is formed by the "third partial flow" of the air downstream of its expansion in the second air turbine. The additional air flow in the cold part of the main heat exchanger makes it possible to achieve a favorable heat exchange diagram and thus to save energy, in particular if nitrogen is obtained as an internally compressed product between 7 and 15 bar.

In vielen Fällen ist eine weitere Optimierung des Wärmeaustauschprozesses im Hauptwärmetauscher möglich, indem ein vierter Teilstrom der im Hauptluftverdichter verdichteten Luft unter dem ersten Druck, dem Austrittsdruck des Hauptluftverdichters, in dem Hauptwärmetauscher abgekühlt und anschließend entspannt und in das Destillationssäulen-System eingeleitet wird.In many cases, further optimization of the heat exchange process in the main heat exchanger is possible by cooling a fourth substream of the compressed air in the main air compressor under the first pressure, the outlet pressure of the main air compressor in the main heat exchanger and then released and introduced into the distillation column system.

Einer der beiden Turbinenströme oder beide können gemeinsam mit dem zweiten Teilstrom in dem ersten Nachverdichter auf den zweiten Druck nachverdichtet werden, wie es in den Patentansprüchen 3 und 4 beschrieben ist.One of the two turbine streams or both can be recompressed together with the second partial flow in the first booster to the second pressure, as described in the claims 3 and 4.

Insbesondere der dritte Teilstrom kann auch ohne Nachverdichtung bleiben; er wird dann unter dem ersten Druck in die zweite Luftturbine eingeleitet.In particular, the third partial flow can remain without recompression; it is then introduced under the first pressure in the second air turbine.

Wenn das System zeitweise mit besonders niedriger Flüssigproduktion oder als reine Gasanlage gefahren werden soll, ist es günstig, zu diesen Zeiten einen zweiten Teil des arbeitsleistend entspannten dritten Teilstroms nicht in den Hauptwärmetauscher einzuführen, sondern in den Verflüssigungsraum einen Sumpfverdampfers der Hochdrucksäule, der als Kondensator-Verdampfer ausgebildet ist.If the system is to be operated at times with particularly low liquid production or as a pure gas system, it is favorable, at these times a second part of the working expanded third partial stream not to introduce into the main heat exchanger, but in the liquefaction room a bottom evaporator of the high-pressure column, which is used as capacitor Evaporator is formed.

Der in dem Verdampfungsraum des Sumpfverdampfers der Hochdrucksäule mindestens teilweise kondensierte Strom wird dann vorzugsweise der Hochdrucksäule an einer Zwischenstelle zugeführt.The stream at least partially condensed in the evaporation space of the bottom evaporator of the high-pressure column is then preferably fed to the high-pressure column at an intermediate point.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand von in den Figuren 1 und 2 schematisch dargestellten Ausführungsbeispielen näher erläutert.The invention and further details of the invention are described below with reference to the FIGS. 1 and 2 illustrated schematically embodiments.

In Figur 1 wird atmosphärische Luft (AIR) wird über ein Filter 1 von einem Hauptluftverdichter 2 angesaugt. Der Hauptluftverdichter weist in dem Beispiel fünf Stufen auf und verdichtet den Gesamtluftstrom auf einen "ersten Druck" von beispielsweise 19,7 bar. Der Gesamtluftstrom 3 stromabwärts des Hauptluftverdichters 2 wird unter dem ersten Druck in einer Vorkühlung 4 gekühlt. Der vorgekühlte Gesamtluftstrom 5 wird in einer Reinigungseinrichtung 6, die insbesondere durch ein Paar umschaltbarer Molsieb-Adsorber gebildet wird, gereinigt. Der gereinigte Gesamtluftstrom 7 wird zu einem ersten Teil 8 in einem im Warmen betriebenen Luftnachverdichter 9 mit Nachkühler 10 auf einen "zweiten Druck" von beispielsweise 24 bar nachverdichtet und anschließend in einen "ersten Teilstrom" 11 (erster Turbinenluftstrom) und einen "zweiten Teilstrom" 12 (erster Drosselstrom) aufgeteilt.In FIG. 1 atmospheric air (AIR) is sucked through a filter 1 from a main air compressor 2. The main air compressor has five stages in the example and compresses the total air flow to a "first pressure", for example 19.7 bar. The total air flow 3 downstream of the main air compressor 2 is cooled under the first pressure in a pre-cooling 4. The pre-cooled total air flow 5 is purified in a cleaning device 6, which is formed in particular by a pair of switchable molecular sieve adsorber. The purified total air flow 7 is recompressed to a first part 8 in a hot air compressor 9 with aftercooler 10 to a "second pressure" of for example 24 bar and then into a "first partial flow" 11 (first turbine air flow) and a "second partial flow". Divided 12 (first inductor current).

Der erste Teilstrom 11 wird in einem Hauptwärmetauscher 13 auf eine erste Zwischentemperatur von ca. 135K abgekühlt. Der abgekühlte erste Teilstrom 14 wird in einer ersten Luftturbine 15 von dem zweiten Druck auf etwa 5,5 bar arbeitsleistend entspannt. Die erste Luftturbine 15 treibt den warmen Luftnachverdichter 9 an. Der arbeitsleistend entspannte erste Teilstrom 16 wird in einen Abscheider (Phasentrenner) 17 eingeleitet. Der flüssige Anteil 18 wird über die Leitungen 19 und 20 in die Niederdrucksäule 22 des Destillationssäulen-Systems eingeleitet.The first substream 11 is cooled in a main heat exchanger 13 to a first intermediate temperature of about 135K. The cooled first partial flow 14 is expanded in a first air turbine 15 from the second pressure to about 5.5 bar to perform work. The first air turbine 15 drives the warm air compressor 9. The work-performing relaxed first partial flow 16 is introduced into a separator (phase separator) 17. The liquid portion 18 is introduced via lines 19 and 20 into the low-pressure column 22 of the distillation column system.

Das Destillationssäulen-System umfasst eine Hochdrucksäule 21, die Niederdrucksäule 22 und einen Hauptkondensator 23 sowie eine übliche Argongewinnung 24 mit Rohargonsäule 25 und Reinargonsäule 26. Der Hauptkondensator 23 ist als Kondensator-Verdampfer ausgebildet, in dem konkreten Beispiel als Kaskadenverdampfer. Der Betriebsdruck am Kopf der Hochdrucksäule beträgt in dem Beispiel 5,3 bar, derjenige am Kopf der Niederdrucksäule 1,35 bar.The distillation column system comprises a high-pressure column 21, the low-pressure column 22 and a main condenser 23 and a conventional argon production 24 with crude argon column 25 and pure argon column 26. The main condenser 23 is designed as a condenser-evaporator, in the concrete example as a cascade evaporator. The operating pressure at the top of the high pressure column is in the example 5.3 bar, the one at the top of the low pressure column 1.35 bar.

Der zweite Teilstrom 12 der Einsatzluft wird in dem Hauptwärmetauscher 13 auf eine zweite Zwischentemperatur abgekühlt, die höher als die erste Zwischentemperatur ist, über Leitung 27 einem Kaltverdichter 28 zugeleitet und dort auf einen "dritten Druck" von ca. 35 bar nachverdichtet. Der nachverdichtete zweite Teilstrom 29 wird bei einer dritten Zwischentemperatur, die höher als die zweite Zwischentemperatur ist, wieder in den Hauptwärmetauscher 13 eingeleitet und dort bis zum kalten Ende abgekühlt. Der kalte zweite Teilstrom 30 wird in einem Drosselventil 31 auf etwa den Betriebsdruck der Hochdrucksäule entspannt und über Leitung 32 der Hochdrucksäule 21 zugeführt. Ein Teil 33 wird wieder entnommen, in einem Unterkühlungs-Gegenströmer 34 abgekühlt und über die Leitungen 35 und 20 in die Niederdrucksäule 22 eingespeist.The second partial flow 12 of the feed air is cooled in the main heat exchanger 13 to a second intermediate temperature, which is higher than the first intermediate temperature, fed via line 27 to a cold compressor 28 and there recompressed to a "third pressure" of about 35 bar. The recompressed second partial stream 29 is at a third intermediate temperature, which is higher than the second intermediate temperature, again introduced into the main heat exchanger 13 and cooled there to the cold end. The cold second partial stream 30 is expanded in a throttle valve 31 to approximately the operating pressure of the high-pressure column and fed via line 32 to the high-pressure column 21. A part 33 is removed again, cooled in a supercooling countercurrent 34 and fed via the lines 35 and 20 in the low-pressure column 22.

Ein "dritter Teilstrom" 436 der Einsatzluft wird unter dem zweiten Druck in den Hauptwärmetauscher 13 eingeleitet und dort auf eine vierte Zwischentemperatur abgekühlt, die in dem Beispiel etwas höher als die erste Zwischentemperatur liegt. Der abgekühlte dritte Teilstrom 37 wird in einer zweiten Luftturbine 38 von dem ersten Druck aus arbeitsleistend entspannt. Der arbeitsleistend entspannte Turbinenstrom 339 weist einen Druck auf, der mindestens 1 bar, insbesondere 4 bis 10 bar über dem Betriebsdruck der Hochdrucksäule liegt, und eine Temperatur, die mindestens 10 K, insbesondere 15 bis 40 K oberhalb der Eintrittstemperatur der Niederdruck-Stickstoffströme 55, 61 am kalten Ende des Hauptwärmetauschers liegt. Dieser Strom wird dann im kalten Teil des Hauptwärmetauschers weiter abgekühlt. Der weiter abgekühlte dritte Teilstrom 340 wird als dritter Drosselstrom in einem Drosselventil 341 auf etwa Hochdrucksäulendruck entspannt und über Leitung 32 in die Hochdrucksäule eingeführt. Hierdurch lässt sich der Wärmeaustauschvorgang im Hauptwärmetauscher weiter optimieren, insbesondere im Falle von relativ geringen GAN-IC-Drücken von beispielsweise 7 bis 15 bar, insbesondere etwa 12 bar.A "third substream" 436 of the feed air is introduced under the second pressure into the main heat exchanger 13 and cooled there to a fourth intermediate temperature, which in the example is slightly higher than the first intermediate temperature. The cooled third partial flow 37 is expanded in a second air turbine 38 from the first pressure to perform work. The working power relaxed turbine stream 339 has a pressure which is at least 1 bar, in particular 4 to 10 bar above the operating pressure of the high-pressure column, and a temperature which is at least 10 K, in particular 15 to 40 K above the inlet temperature of the low-pressure nitrogen streams 55, 61 is located at the cold end of the main heat exchanger. This stream is then further cooled in the cold part of the main heat exchanger. The further cooled third partial flow 340 is expanded as a third throttle flow in a throttle valve 341 to about high-pressure column pressure and introduced via line 32 into the high-pressure column. As a result, the heat exchange process in the main heat exchanger can be further optimized, in particular in the case of relatively low GAN-IC pressures of for example 7 to 15 bar, in particular about 12 bar.

Die zweite Luftturbine 38 treibt den Kaltverdichter 28 an. Der arbeitsleistend entspannte dritte Teilstrom 339 wird über Leitung 40 der Hochdrucksäule 21 am Sumpf zugeführt.The second air turbine 38 drives the cold compressor 28. The working expanded third partial flow 339 is supplied via line 40 of the high-pressure column 21 at the bottom.

(Die Aufteilung in die Teilströme gleichen Drucks könnte abweichend von der Darstellung in der Zeichnung von Figur 1 auch im Inneren des Hauptwärmetauschers 13 durchgeführt werden.)(The division into the partial flows of equal pressure could deviate from the representation in the drawing of FIG. 1 also be performed inside the main heat exchanger 13.)

Ein "vierter Teilstrom" 41 (zweiter Drosselstrom) durchströmt den Hauptwärmetauscher 13 vom warmen bis zum kalten Ende unter dem ersten Druck. Der kalte vierte Teilstrom 42 wird in einem Drosselventil 43 auf etwa den Betriebsdruck der Hochdrucksäule entspannt und über Leitung 32 der Hochdrucksäule 21 zugeführt.A "fourth partial flow" 41 (second throttle flow) flows through the main heat exchanger 13 from the hot to the cold end under the first pressure. The cold fourth partial stream 42 is expanded in a throttle valve 43 to approximately the operating pressure of the high-pressure column and fed via line 32 to the high-pressure column 21.

Die sauerstoffangereicherte Sumpfflüssigkeit 44 der Hochdrucksäule 21 wird im Unterkühlungs-Gegenströmer 34 abgekühlt und über Leitung 45 in die fakultative Argongewinnung 24 eingeleitet. Daraus erzeugter Dampf 46 und verbleibende Flüssigkeit 47 werden in die Niederdrucksäule 22 eingespeist.The oxygen-enriched bottom liquid 44 of the high-pressure column 21 is cooled in the subcooling countercurrent 34 and introduced via line 45 into the optional argon recovery 24. Resulting vapor 46 and remaining liquid 47 are fed into the low-pressure column 22.

Ein erster Teil 49 des Kopfstickstoffs 48 der Hochdrucksäule 21 wird im Verflüssigungsraum des Hauptkondensators 23 gegen im Verdampfungsraum verdampfenden flüssigen Sauerstoff aus dem Sumpf der Niederdrucksäule vollständig oder im Wesentlichen vollständig verflüssigt. Ein erster Teil 51 des dabei erzeugten flüssigen Stickstoffs 50 wird als Rücklauf auf die Hochdrucksäule 21 aufgegeben. Ein zweiter Teil 52 wird im Unterkühlungs-Gegenströmer 34 abgekühlt, über Leitung 53 in die Niederdrucksäule 22 eingespeist. Mindestens ein Teil des flüssigen Niederdruckstickstoffs 53 dient als Rücklauf in der Niederdrucksäule 21; ein anderer Teil 54 kann als Flüssigstickstoffprodukt (LIN) gewonnen werden.A first part 49 of the top nitrogen 48 of the high-pressure column 21 is completely or substantially completely liquefied in the liquefaction space of the main condenser 23 against liquid oxygen evaporating in the evaporation space from the bottom of the low-pressure column. A first part 51 of the liquid nitrogen 50 produced in the process is introduced as reflux to the high-pressure column 21. A second part 52 is cooled in the subcooling countercurrent 34, fed via line 53 into the low pressure column 22. At least a portion of the liquid low pressure nitrogen 53 serves as reflux in the low pressure column 21; another part 54 can be obtained as liquid nitrogen product (LIN).

Von einer Zwischenstelle der Niederdrucksäule 22 wird gasförmiger Unreinstickstoff 61 abgezogen, im Unterkühlungs-Gegenströmer 34 und im Hauptwärmetauscher 13 angewärmt. Der warme Unreinstickstoff 62 kann in die Atmosphäre (ATM) abgeblasen (63) und/oder als Regeneriergas 64 für die Reinigungseinrichtung 6 eingesetzt werden. Gasförmiger Stickstoff 55 vom Kopf der Niederdrucksäule 22 wird ebenfalls im Unterkühlungs-Gegenströmer 34 und im Hauptwärmetauscher 13 angewärmt und über Leitung 56 als Niederdruckstickstoffprodukt (GAN) abgezogen.From an intermediate point of the low pressure column 22 gaseous impurity nitrogen 61 is withdrawn, warmed in the supercooling countercurrent 34 and in the main heat exchanger 13. The warm impure nitrogen 62 may be vented (63) into the atmosphere (ATM) and / or used as the regeneration gas 64 for the purifier 6. Gaseous nitrogen 55 from the top of the low pressure column 22 is also heated in the subcooling countercurrent 34 and main heat exchanger 13 and withdrawn via line 56 as low pressure nitrogen product (GAN).

Die Leitungen 67 und 68 (sogenannter Argonübergang) verbinden die Niederdrucksäule 21 mit der Rohargonsäule 25 der Argongewinnung 24.The lines 67 and 68 (so-called argon transition) connect the low-pressure column 21 with the crude argon column 25 of argon recovery 24th

Ein erster Teil 70 des flüssigen Sauerstoffs 69 vom Sumpf der Niederdrucksäule 21 wird als "erster Produktstrom" abgezogen, in einer Sauerstoffpumpe 71 auf einen "ersten Produktdruck" von beispielsweise 37 bar gebracht und unter dem ersten Produktdruck in dem Hauptwärmetauscher 13 verdampft und schließlich über Leitung 72 als "erstes Druckgasprodukt" (GOX IC - innenverdichteter gasförmiger Sauerstoff) gewonnen.A first portion 70 of the liquid oxygen 69 from the bottom of the low-pressure column 21 is withdrawn as the "first product stream", brought to a "first product pressure" of, for example, 37 bar in an oxygen pump 71 and vaporized under the first product pressure in the main heat exchanger 13 and finally via line 72 as "first compressed gas product" (GOX IC - compressed gas internal oxygen) won.

Ein zweiter Teil 73 des flüssigen Sauerstoffs 69 vom Sumpf der Niederdrucksäule 21 wird gegebenenfalls im Unterkühlungs-Gegenströmer 34 abgekühlt und über Leitung 74 als Flüssigsauerstoffprodukt (LOX) gewonnen.A second portion 73 of the liquid oxygen 69 from the bottom of the low-pressure column 21 is optionally cooled in the subcooling countercurrent 34 and recovered via line 74 as a liquid oxygen product (LOX).

In dem Beispiel wird auch ein dritter Teil 75 des flüssigen Stickstoffs 50 aus der Hochdrucksäule 21 beziehungsweise dem Hauptkondensator 23 einer Innenverdichtung unterzogen, indem er in einer Stickstoffpumpe 76 auf einen zweiten Produktdruck von beispielsweise 12 bar gebracht, unter dem zweiten Produktdruck in dem Hauptwärmetauscher 13 pseudo-verdampft und schließlich über Leitung 77 als innenverdichtetes gasförmiges Stickstoff-Druckprodukt (GAN IC) gewonnen.In the example, a third part 75 of the liquid nitrogen 50 from the high-pressure column 21 and the main condenser 23 is also subjected to internal compression by being brought in a nitrogen pump 76 to a second product pressure of 12 bar, for example, under the second product pressure in the main heat exchanger 13 pseudo and finally recovered via line 77 as internally compressed gaseous nitrogen pressure product (GAN IC).

Ein zweiter Teil 78 des gasförmigen Kopfstickstoffs 48 der Hochdrucksäule 21 wird im Hauptwärmetauscher angewärmt und über Leitung 79 entweder als gasförmiges Mitteldruckprodukt gewonnen oder - wie dargestellt - als Dichtgas (Sealgas) für eine oder mehrere der dargestellten Prozesspumpen eingesetzt.A second part 78 of the gaseous top nitrogen 48 of the high-pressure column 21 is warmed in the main heat exchanger and recovered via line 79 either as a gaseous medium pressure product or - as shown - used as a sealing gas (seal gas) for one or more of the illustrated process pumps.

Figur 2 unterscheidet sich von Figur 1 dadurch, dass der dritte Teilstrom 36 der Einsatzluft unter dem ersten Druck in den Hauptwärmetauscher 13 eingeleitet wird und die zweite Turbine 38 damit einen entsprechend niedrigeren Eintrittsdruck hat. FIG. 2 differs from FIG. 1 in that the third partial flow 36 of the feed air is introduced under the first pressure into the main heat exchanger 13 and the second turbine 38 thus has a correspondingly lower inlet pressure.

In dem Ausführungsbeispiel der Figur 3 weist die Hochdrucksäule einen Sumpfverdampfer 351 auf. Dieser wird insbesondere dann eingesetzt, wenn mindestens zeitweise eine besonders niedrige Flüssigproduktion oder sogar reiner Gasbetrieb gewünscht ist. Die Turbine 38 der vorigen Ausführungsbeispiele kann nicht mit ihrem maximalen Durchsatz gefahren werden, weil ansonsten zu viel Luft als dritter Teilstrom durch das kalte Ende des Hauptwärmetauschers gefahren werden müsste und der Betrieb des Hauptwärmetauschers damit weniger effizient wäre.In the embodiment of FIG. 3 the high-pressure column has a sump evaporator 351. This is used in particular when at least temporarily a particularly low liquid production or even pure gas operation is desired. The turbine 38 of the previous embodiments can not be driven with their maximum throughput, because otherwise too much air would have to be driven as a third partial flow through the cold end of the main heat exchanger and the operation of the main heat exchanger would be less efficient.

In Figur 3 kann nun bei besonders niedriger Flüssigproduktion ein Teil 350 des dritten Teilstroms aus der Turbine 38 am Hauptwärmetauscher vorbeigeführt werden. Die Turbine 38 (und damit der gekoppelte Kaltverdichter) kann nun mit vollen Durchsatz gefahren werden, ohne den Wärmeaustauschvorgang im Hauptwärmetauscher zu belasten. Der Strom 350 wird im Verdampfungsraum des Sumpfverdampfers 351 mindestens teilweise kondensiert und anschließend über Leitung 352 der Hochdrucksäule an einer Zwischenstelle zugeführt. Er verstärkt damit die Destillation im unteren Teil der Hochdrucksäule.In FIG. 3 can now be passed at a particularly low liquid production part 350 of the third partial flow from the turbine 38 on the main heat exchanger. The turbine 38 (and thus the coupled cold compressor) can now be operated at full throughput, without burdening the heat exchange process in the main heat exchanger. The stream 350 is at least partially condensed in the evaporation space of the bottom evaporator 351 and then via line 352 of High-pressure column fed at an intermediate point. He intensifies the distillation in the lower part of the high-pressure column.

Abweichend von der Darstellung in Figur 3 kann der Strom 350 auch vor der Einleitung in den Sumpfverdampfer im Hauptwärmetauscher auf den Tauzustand abgekühlt werden. Dies kann in einer separaten Passage erfolgen, aber auch durch Zwischenentnahme an geeigneter Stelle und entsprechende Umspeisung.Deviating from the illustration in FIG. 3 For example, the stream 350 can also be cooled to the dew state before it is introduced into the bottom evaporator in the main heat exchanger. This can be done in a separate passage, but also by intermediate removal at a suitable location and appropriate Umspeisung.

Claims (8)

Verfahren zur Gewinnung eines Druckgasprodukts (72; 73) mittels Tieftemperaturzerlegung von Luft in einem Destillationssäulen-System, das eine Hochdrucksäule (21) und eine Niederdrucksäule (22) aufweist, bei dem - die gesamte Einsatzluft in einem Hauptluftverdichter (2) auf einen ersten Druck verdichtet wird, der mindestens 4 bar höher als der Betriebsdruck der Hochdrucksäule (21) ist, - ein erster Teilstrom (8, 11, 14) der im Hauptluftverdichter (2) verdichteten Einsatzluft (7) in einem Hauptwärmetauscher (13) auf eine Zwischentemperatur abgekühlt und in einer ersten Luftturbine (15) arbeitsleistend entspannt wird, - mindestens ein erster Teil des arbeitsleistend entspannten ersten Teilstroms (16) in das Destillationssäulen-System eingeleitet (40; 18, 19, 20) wird, - ein zweiter Teilstrom (12, 27, 29, 30) der im Hauptluftverdichter (2) verdichteten Einsatzluft in einem ersten Nachverdichter (9), der insbesondere von der ersten Turbine (15) angetrieben wird, auf einen zweiten Druck nachverdichtet wird, der höher als der erste Druck ist, in dem Hauptwärmetauscher (13) auf eine Zwischentemperatur abgekühlt, in einem zweiten Nachverdichter (28), der als Kaltverdichter betrieben und insbesondere von der zweiten Turbine (38) angetrieben wird, auf einen dritten Druck nachverdichtet wird, der höher als der zweite Druck ist, in dem Hauptwärmetauscher (13) abgekühlt und anschließend entspannt (31) und in das Destillationssäulen-System eingeleitet (32) wird, - ein dritter Teilstrom (436, 37) der im Hauptluftverdichter (2) verdichteten Einsatzluft (7) in dem Hauptwärmetauscher (13) auf eine Zwischentemperatur abgekühlt und in einer zweiten Luftturbine (38) arbeitsleistend entspannt wird und - mindestens ein erster Teil (339) des arbeitsleistend entspannten dritten Teilstroms in das Destillationssäulen-System eingeleitet (340) wird, - ein erster Produktstrom (69; 75) flüssig aus dem Destillationssäulen-System entnommen und einer Druckerhöhung (71; 76) auf einen ersten Produktdruck unterworfen wird, - der erste Produktstrom unter dem ersten Produktdruck im Hauptwärmetauscher (13) verdampft oder pseudo-verdampft und angewärmt wird und - der angewärmte erste Produktstrom (72; 77) als erstes Druckgasprodukt (GOX IC; GAN IC) gewonnen wird,
dadurch gekennzeichnet, dass - der dritte Teilstrom (37) in der zweiten Luftturbine (38) auf einen Druck entspannt wird, der mindestens 1 bar höher als der Betriebsdruck der Hochdrucksäule (21) ist, - der Eintrittsdruck der ersten Luftturbine (15) mindestens ein 1 bar kleiner als der dritte Druck ist und - mindestens ein erster Teil (339) des arbeitsleistend entspannten dritten Teilstroms in dem Hauptwärmetauscher (13) weiter abgekühlt, verflüssigt und anschließend entspannt (341) und in das Destillationssäulen-System eingeleitet wird. A process for recovering a compressed gas product (72; 73) by cryogenic separation of air in a distillation column system comprising a high pressure column (21) and a low pressure column (22), wherein - the total feed air in a main air compressor (2) is compressed to a first pressure which is at least 4 bar higher than the operating pressure of the high-pressure column (21), a first partial flow (8, 11, 14) of the feed air (7) compressed in the main air compressor (2) is cooled to an intermediate temperature in a main heat exchanger (13) and expanded in a first air turbine (15) to perform work, at least a first part of the work-performing expanded first partial flow (16) is introduced into the distillation column system (40, 18, 19, 20), - A second partial stream (12, 27, 29, 30) of the main air compressor (2) compressed feed air in a first booster (9), which is in particular from the first turbine (15) is driven to a second pressure is recompressed, the higher as the first pressure is, in the main heat exchanger (13) cooled to an intermediate temperature, in a second booster (28) operated as a cold compressor and in particular by the second turbine (38) is recompressed to a third pressure, the higher when the second pressure is cooled in the main heat exchanger (13) and then expanded (31) and introduced into the distillation column system (32), - A third partial stream (436, 37) of the compressed air in the main compressor (2) compressed air (7) in the main heat exchanger (13) to an intermediate temperature and in a second air turbine (38) is expanded to perform work and - at least a first part (339) of the work-performing expanded third substream is introduced into the distillation column system (340), a first product stream (69; 75) is removed from the distillation column system in liquid form and subjected to a pressure increase (71; 76) to a first product pressure, - The first product stream under the first product pressure in the main heat exchanger (13) is evaporated or pseudo-evaporated and warmed and the warmed first product stream (72; 77) is obtained as the first compressed gas product (GOX IC; GAN IC),
characterized in that the third partial flow (37) in the second air turbine (38) is expanded to a pressure which is at least 1 bar higher than the operating pressure of the high-pressure column (21), - The inlet pressure of the first air turbine (15) is at least a 1 bar less than the third pressure and - At least a first part (339) of the work-performing expanded third partial flow in the main heat exchanger (13) further cooled, liquefied and then relaxed (341) and introduced into the distillation column system. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass ein vierter Teilstrom (41, 42) der im Hauptluftverdichter (2) verdichteten Luft (7) unter dem ersten Druck in dem Hauptwärmetauscher (13) abgekühlt und anschließend entspannt (43) und in das Destillationssäulen-System eingeleitet wird.A method according to claim 1, characterized in that a fourth substream (41, 42) of the compressed air in the main air compressor (2) (7) under the first pressure in the main heat exchanger (13) and then expanded (43) and in the Destillationssäulen- System is initiated. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass der erste Teilstrom gemeinsam mit dem zweiten Teilstrom in dem erste Nachverdichter (9) auf den zweiten Druck gebracht wird und unter dem zweiten Druck in die erste Luftturbine (15) eingeleitet wird.A method according to claim 1 or 2, characterized in that the first partial flow is brought together with the second partial flow in the first booster (9) to the second pressure and is introduced under the second pressure in the first air turbine (15). Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass der dritte Teilstrom gemeinsam mit dem zweiten Teilstrom und gegebenenfalls mit dem ersten Teilstrom in dem ersten Nachverdichter (9) auf den zweiten Druck gebracht wird und unter dem zweiten Druck in die zweite Luftturbine (38) eingeleitet wird.Method according to one of claims 1 to 3, characterized in that the third partial flow is brought together with the second partial flow and optionally with the first partial flow in the first booster (9) to the second pressure and under the second pressure in the second air turbine ( 38) is initiated. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass der dritte Teilstrom unter dem ersten Druck in die zweite Luftturbine (38) eingeleitet wird.Method according to one of claims 1 to 3, characterized in that the third partial flow is introduced under the first pressure in the second air turbine (38). Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass zumindest zeitweise ein zweiter Teil (350) des arbeitsleistend entspannten dritten Teilstroms nicht in den Hauptwärmetauscher (13) eingeführt wird, sondern in den Verflüssigungsraum einen Sumpfverdampfers (351) der Hochdrucksäule, der als Kondensator-Verdampfer ausgebildet ist.Method according to one of claims 1 to 5, characterized in that at least temporarily a second part (350) of the work-performing expanded third partial flow is not introduced into the main heat exchanger (13), but in the Liquefaction space a sump evaporator (351) of the high-pressure column, which is designed as a condenser-evaporator. Verfahren nach Anspruch 6, dadurch gekennzeichnet, dass der in dem Verdampfungsraum des Sumpfverdampfers (351) der Hochdrucksäule mindestens teilweise kondensierte Strom (352) der Hochdrucksäule an einer Zwischenstelle zugeführt wird.A method according to claim 6, characterized in that in the evaporation space of the bottom evaporator (351) of the high-pressure column at least partially condensed stream (352) of the high-pressure column is fed at an intermediate point. Vorrichtung zur Gewinnung eines Druckgasprodukts (72; 73) mittels Tieftemperaturzerlegung von Luft mit - einem Destillationssäulen-System, das eine Hochdrucksäule (21) und eine Niederdrucksäule (22) aufweist, - einem Hauptluftverdichter (2) zum Verdichten der gesamten Einsatzluft auf einen ersten Druck, der mindestens 4 bar höher als der Betriebsdruck der Hochdrucksäule (21) ist, - Mittel zum Abkühlen eines ersten Teilstroms (8, 11, 14) der im Hauptluftverdichter (2) verdichteten Einsatzluft (7) in einem Hauptwärmetauscher (13) auf eine Zwischentemperatur - Mittel zum Einleiten des auf die Zwischentemperatur abgekühlten ersten Teilstroms in eine erste Luftturbine (15), - Mittel (40; 18, 19, 20) zum Einleiten des in der ersten Luftturbine (15) arbeitsleistend entspannten ersten Teilstroms (16) in das Destillationssäulen-System, - einem ersten Nachverdichter (9), der insbesondere von der ersten Turbine (15) angetrieben wird, zum Nachverdichten eines zweiten Teilstroms (12, 27, 29, 30) der im Hauptluftverdichter (2) verdichteten Einsatzluft auf einen zweiten Druck, der höher als der erste Druck ist, - Mittel zum Abkühlen des nachverdichteten zweiten Teilstroms in dem Hauptwärmetauscher (13) auf eine Zwischentemperatur, - einem zweiten Nachverdichter (28), der als Kaltverdichter betrieben und insbesondere von der zweiten Turbine (38) angetrieben wird, zum Nachverdichten des zweiten Teilstroms auf einen dritten Druck, der höher als der zweite Druck ist, - Mittel zum Abkühlen des weitere nachverdichteten zweiten Teilstroms in dem Hauptwärmetauscher (13) und zum anschließenden Entspannen (31) und Einleiten (32) in das Destillationssäulen-System eingeleitet wird, - Mittel zum Abkühlen eines dritten Teilstroms (436, 37) der im Hauptluftverdichter (2) verdichteten Einsatzluft (7) in dem Hauptwärmetauscher (13) auf eine Zwischentemperatur, - einer zweiten Luftturbine (38) zum arbeitsleistenden Entspannen des abgekühlten dritten Teilstroms, - Mittel zum Einleiten (340) des arbeitsleistend entspannten dritten Teilstroms in das Destillationssäulen-System, - Mittel zum flüssigen Entnehmen eines ersten Produktstroms (69; 75) aus dem Destillationssäulen-System, - Mittel zur Druckerhöhung (71; 76) des flüssig entnommenen ernste Produktstroms (69; 75) auf einen ersten Produktdruck, - Mittel zur Verdampfung und Pseudo-Verdampfung des ersten Produktstroms unter dem ersten Produktdruck im Hauptwärmetauscher (13) und mit - Mittel zum Gewinnen des angewärmten erste Produktstroms (72; 77) als erstes Druckgasprodukt (GOX IC; GAN IC),
gekennzeichnet durch - Regelungsmittel zur Einstellung des Austrittsdrucks der zweiten Luftturbine (38) auf einen Druck, der mindestens 1 bar höher als der Betriebsdruck der Hochdrucksäule (21) ist, - Mittel zum Einleiten des ersten Teilstroms in die erste Luftturbine (15) unter einem Eintrittsdruck, der mindestens ein 1 bar kleiner als der dritte Druck ist, - Mittel zum Einleiten des arbeitsleistend entspannten dritten Teilstroms (399) in den Hauptwärmetauscher (13) zum Abkühlen und Verflüssigen und durch - Mittel zum Entspannen (341) und Einleiten in das Destillationssäulen-System des verflüssigten dritten Teilstroms. Apparatus for recovering a compressed gas product (72, 73) by means of cryogenic separation of air with a distillation column system comprising a high pressure column (21) and a low pressure column (22), - A main air compressor (2) for compressing the total feed air to a first pressure which is at least 4 bar higher than the operating pressure of the high-pressure column (21), - means for cooling a first partial flow (8, 11, 14) of the main air compressor (2) compressed feed air (7) in a main heat exchanger (13) to an intermediate temperature Means for introducing the first partial flow cooled to the intermediate temperature into a first air turbine (15), Means (40; 18, 19, 20) for introducing the first partial flow (16), which in the first air turbine (15) performs work, into the distillation column system, - A first post-compressor (9), which is driven in particular by the first turbine (15), for recompressing a second partial flow (12, 27, 29, 30) of the main air compressor (2) compressed feed air to a second pressure higher than the first pressure is Means for cooling the post-compressed second substream in the main heat exchanger (13) to an intermediate temperature, a second after-compressor (28), which is operated as a cold compressor and in particular driven by the second turbine (38), for recompressing the second partial flow to a third pressure, which is higher than the second pressure, - means for cooling the further recompressed second substream in the main heat exchanger (13) and for subsequent expansion (31) and introduction (32) is introduced into the distillation column system, Means for cooling a third partial flow (436, 37) of the feed air (7) compressed in the main air compressor (2) in the main heat exchanger (13) to an intermediate temperature, - a second air turbine (38) for work-performing expansion of the cooled third partial flow, Means for introducing (340) the work-performing expanded third substream into the distillation column system, - means for liquid withdrawal of a first product stream (69; 75) from the distillation column system, - means for increasing the pressure (71; 76) of the liquid withdrawn serious product stream (69; 75) to a first product pressure, - means for evaporation and pseudo-evaporation of the first product stream under the first product pressure in the main heat exchanger (13) and with Means for obtaining the warmed first product stream (72, 77) as the first compressed gas product (GOX IC, GAN IC),
marked by - Control means for adjusting the outlet pressure of the second air turbine (38) to a pressure which is at least 1 bar higher than the operating pressure of the high-pressure column (21), Means for introducing the first partial flow into the first air turbine (15) at an inlet pressure which is at least 1 bar less than the third pressure, - Means for introducing the working expanded third partial flow (399) in the main heat exchanger (13) for cooling and liquefying and by - means for expansion (341) and introduction into the distillation column system of the liquefied third substream.
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