EP2963367A1 - Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch - Google Patents

Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch Download PDF

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Publication number
EP2963367A1
EP2963367A1 EP14002307.8A EP14002307A EP2963367A1 EP 2963367 A1 EP2963367 A1 EP 2963367A1 EP 14002307 A EP14002307 A EP 14002307A EP 2963367 A1 EP2963367 A1 EP 2963367A1
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EP
European Patent Office
Prior art keywords
pressure
compressor
air
compressed
stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP14002307.8A
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German (de)
English (en)
French (fr)
Inventor
Dimitri Goloubev
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP14002307.8A priority Critical patent/EP2963367A1/de
Priority to EP15735849.0A priority patent/EP3164654B1/de
Priority to CN201580036802.0A priority patent/CN106489059B/zh
Priority to RU2017103309A priority patent/RU2690550C2/ru
Priority to RU2017103099A priority patent/RU2691210C2/ru
Priority to EP15733625.6A priority patent/EP3164653A1/de
Priority to US15/322,740 priority patent/US10215489B2/en
Priority to CN201580036844.4A priority patent/CN106662394B/zh
Priority to PCT/EP2015/001284 priority patent/WO2016005030A1/de
Priority to US15/322,468 priority patent/US10458702B2/en
Priority to PCT/EP2015/001285 priority patent/WO2016005031A1/de
Priority to TW104121752A priority patent/TW201607599A/zh
Priority to TW104121751A priority patent/TW201607598A/zh
Publication of EP2963367A1 publication Critical patent/EP2963367A1/de
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • 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
    • F25J3/04024—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
    • 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
    • F25J3/0403—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—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
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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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—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
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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
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    • F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
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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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    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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.
  • a product stream brought to liquid pressure is vaporized against a heat carrier 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 frequently replaced by a part of Air formed, in the present case of 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 all of the feed air is at a pressure well above the highest distillation pressure prevailing inside the columns of the distillation column system (normally, this compresses the high pressure column pressure.)
  • Such systems are also referred to as HAP processes
  • the "first pressure”, ie the outlet pressure of the main air compressor (MAC), in which the total air is compressed, is for example more than 4 bar, in particular 6 to 16 bar above that absolutely, the "first pressure” is, for example, 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 here to mean a single-stage or multistage compressor whose stages are all connected to the same drive, all stages being accommodated in the same housing or connected to the same gear.
  • 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 has for its object to provide a method and a corresponding device, which combine the advantages of HAP method with a flexibility, as is similar in MAC-BAC method known.
  • "Flexibility" is understood here in particular that the system can be operated not only energetically favorable at a certain production amount of internally compressed product, but in a relatively wide load range at approximately constant low specific energy consumption. In particular, the production of other air separation products should remain the same or at least change less than the product quantity of the internal compaction product.
  • a portion of the feed air amount or a nitrogen-enriched process stream bypasses the low pressure column or the entire distillation column system, respectively. This amount then does not participate in the production of the first product stream, but can still be passed through the first turbine, so as to produce enough cold or to supply enough energy into the system to maintain liquid production, or at least relatively less as the amount of the first print production.
  • a low-pressure GAN compressor is provided as a nitrogen product compressor in the process, for example because of large amounts of nitrogen product, this can be relieved by interim feeding of pressure GAN from the high-pressure column.
  • this pressure GAN is fed into the nitrogen product compressor at an appropriate point (for example after the second or third compressor stage).
  • the proportion of low-pressure GAN (the amount of gas to be compressed from approximately atmospheric pressure to approximately 5 bar) can be correspondingly reduced.
  • the second process stream can also be mixed with the first process stream at the inlet of a nitrogen product compressor. In many cases, however, it is favorable if the mixing of the second with the first process stream or the fourth with the second process stream is carried out at an intermediate stage of the multistage compressor or the nitrogen product compressor.
  • an oxygen gas stream may be withdrawn from the lower region of the low pressure column, mixed with a nitrogen-enriched stream from the top of the low pressure column, and the mixture heated in the main heat exchanger.
  • a second air turbine can be used, wherein a third part of the stream compressed in the main air compressor feed air is cooled to an intermediate temperature in a main heat exchanger and expanded work in the second air turbine and at least a first part of the working expanded third partial flow in the Distillation column system is initiated.
  • the second part-stream of the feed air compressed in the main air compressor can be cooled to an intermediate temperature in the main heat exchanger, be recompressed to a third pressure that is higher than the first pressure in a second after-compressor, operated as a cold compressor and driven by the second turbine, cooled in the main heat exchanger, (pseudo) liquefied and then released and introduced into the distillation column system.
  • a second after-compressor operated as a cold compressor and driven by the second turbine
  • cooled in the main heat exchanger cooled in the main heat exchanger, (pseudo) liquefied and then released and introduced into the distillation column system.
  • a fourth substream of the compressed air in the main air compressor can be cooled below the first pressure in the main heat exchanger and then released and introduced into the distillation column system.
  • the third partial flow is relaxed in the second air turbine to a pressure which is at least 1 bar higher than the operating pressure of the high-pressure column, and the working expanded third partial stream in the main heat exchanger further cooled and then depressurized and introduced into the distillation column system.
  • a third throttle flow of the heat exchange process in the main heat exchanger is further optimized.
  • the amount of feed air in the cold box is "artificially" raised, that is, more air is driven into the cryogenic part of the system than is necessary to obtain the specified for this operating case pressure oxygen products. If one moves the feed air in the "excess", the pressure at the compressor outlet can be reduced, since the energy supply for the (Pseudo-) evaporation of the GOXIV product is then done not with the air pressure, but with the amount of air.
  • the first partial flow of the feed air compressed in the main air compressor is recompressed upstream of its introduction into the main heat exchanger in a first after-compressor which is operated warm and in particular is driven by the first turbine.
  • the inlet pressure of the first turbine is significantly higher than the first pressure to which the total air is compressed.
  • the air for the second turbine is not recompressed, that is, its inlet pressure is at the lower level of the first pressure.
  • the invention also relates to a device according to claim 13.
  • the device according to the invention can be supplemented by device features which correspond to the features of the dependent method claims.
  • the "means for switching between a first and a second mode of operation" are complex control devices which, in conjunction, enable at least partial automatic switching between the two modes of operation, for example by means of a suitably programmed operational control system.
  • Atmospheric air is drawn in via 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" of for example 22 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, 28 bar and then into a "first partial flow” 11 (first turbine air flow) and a "second partial flow” 12 (FIG. first inductor current) divided.
  • the first partial flow 11 is cooled in a main heat exchanger 13 to a first intermediate temperature.
  • 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 in 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 stream 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 40 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" 36 of the feed air is introduced under the first pressure in the main heat exchanger 13 and cooled there to a fourth intermediate temperature, which is slightly lower than the first intermediate temperature in the example.
  • the cooled third partial flow 37 is expanded in a second air turbine 37 from the first pressure to about high-pressure column pressure to perform work.
  • the second air turbine 38 drives the cold compressor 28.
  • the working expanded third partial stream 39 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 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 in the liquefaction space of the main condenser 23 against evaporating in the evaporation space liquid oxygen from the bottom of the low pressure column completely or substantially completely liquefied.
  • a first part 51 of the liquid nitrogen 51 produced in this 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 low-pressure nitrogen 55 is withdrawn, warmed in the supercooling countercurrent 34 and in the main heat exchanger 13.
  • the warm low-pressure nitrogen 56 is compressed in a two-section nitrogen product compressor (57, 59) with intermediate and after-cooling (58, 60) to the desired product pressure, which in the example is 12 bar.
  • the first section 57 of the nitrogen product compressor consists for example of two or three stages with associated aftercoolers; the second section 59 has at least one step and is preferably also intermediate and post-cooled.
  • gaseous impurity nitrogen 55 is withdrawn, warmed in the subcooling countercurrent 34 and 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.
  • 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 37 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.
  • a lower oxygen production (for example 75%) may then be considered a "second mode of operation".
  • part of the gaseous portion 17 of the work-performing expanded first partial flow 16 is returned as "second process stream" via the lines 65, 66 through the main heat exchanger to an intermediate stage of the main air compressor 2.
  • the recirculation flow between the second and the third stage and between the third and fourth stage of the main air compressor is added to the feed air.
  • This feed air is in the first variant of the invention, the "first process stream".
  • a 95% operation could be considered a "first mode of operation”.
  • a “second mode of operation” is then achieved, for example, with an oxygen production of 90% of the design value.
  • the recirculation quantity in the table refers to the current air volume through filter 1. All percentages here and in the rest of the text refer to molar quantities, unless stated otherwise.
  • FIG. 2 an embodiment of the second variant of the invention is shown. It is different from FIG. 1 by the following features.
  • the corresponding amount of nitrogen 180 from the high pressure column is not condensed in the main condenser 23 and not introduced into the low pressure column. As a result, it does not participate in the rectification in the low-pressure column (neither indirectly via the evaporation of the sump oxygen, nor directly by use as reflux liquid) and thereby enables the reduction of oxygen production. At the same time, the same amount of air (or only slightly less) is available for refrigeration and nitrogen production.
  • FIG. 1 The flexibility of the method can be further increased by the optional measure described below (which basically also applies to the first variant) FIG. 1 can be used).
  • gaseous oxygen 181 is withdrawn from the low pressure column and with the gaseous impurity nitrogen 61 mixed from the low pressure column.
  • the mixing takes place in the example downstream of the subcooling countercurrent 34.
  • the conduit 181 is closed or less gas is supplied via conduit 181.
  • the following table shows example numerical values of two different operating modes of the system FIG. 2 at: GOX IC amount 72 Air volume through main air compressor 2 Amount of nitrogen through line 180 Amount of oxygen through line 181 100% 100% 0% 0% 76% 83% 5% 0%
  • the amount of nitrogen through line 180 refers to the amount of air through filter 1 in the design case.
  • FIG. 3 differs from FIG. 1 through a third inductor current.
  • the second turbine 38 is operated with a relatively large outlet pressure and a relatively high outlet temperature.
  • the work-expanded turbine stream 339 then has a pressure which is at least 1 bar, in particular 4 to 11 bar above the operating pressure of the high-pressure column, and a temperature which is at least 10 K, in particular 20 to 60 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.

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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)
EP14002307.8A 2014-07-05 2014-07-05 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch Withdrawn EP2963367A1 (de)

Priority Applications (13)

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EP14002307.8A EP2963367A1 (de) 2014-07-05 2014-07-05 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch
EP15735849.0A EP3164654B1 (de) 2014-07-05 2015-06-25 Verfahren und vorrichtung zur tieftemperaturzerlegung von luft mit variablem energieverbrauch
CN201580036802.0A CN106489059B (zh) 2014-07-05 2015-06-25 以可变能耗低温分离空气的方法和设备
RU2017103309A RU2690550C2 (ru) 2014-07-05 2015-06-25 Способ и устройство для низкотемпературного разделения воздуха с переменным потреблением энергии
RU2017103099A RU2691210C2 (ru) 2014-07-05 2015-06-25 Способ и устройство для низкотемпературного разделения воздуха с переменным потреблением энергии
EP15733625.6A EP3164653A1 (de) 2014-07-05 2015-06-25 Verfahren und vorrichtung zur tieftemperaturzerlegung von luft mit variablem energieverbrauch
US15/322,740 US10215489B2 (en) 2014-07-05 2015-06-25 Method and device for the low-temperature separation of air at variable energy consumption
CN201580036844.4A CN106662394B (zh) 2014-07-05 2015-06-25 以可变能耗低温分离空气的方法和设备
PCT/EP2015/001284 WO2016005030A1 (de) 2014-07-05 2015-06-25 Verfahren und vorrichtung zur tieftemperaturzerlegung von luft mit variablem energieverbrauch
US15/322,468 US10458702B2 (en) 2014-07-05 2015-06-25 Method and device for the low-temperature separation of air at variable energy consumption
PCT/EP2015/001285 WO2016005031A1 (de) 2014-07-05 2015-06-25 Verfahren und vorrichtung zur tieftemperaturzerlegung von luft mit variablem energieverbrauch
TW104121752A TW201607599A (zh) 2014-07-05 2015-07-03 以可變能耗低溫分離空氣之方法與裝置
TW104121751A TW201607598A (zh) 2014-07-05 2015-07-03 以可變能耗低溫分離空氣之方法與裝置

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CN114674112A (zh) * 2022-04-07 2022-06-28 安阳钢铁股份有限公司 一种液化装置氧氮自动转换方法

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US10458702B2 (en) 2019-10-29
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EP3164654A1 (de) 2017-05-10
US20170153058A1 (en) 2017-06-01
RU2017103309A (ru) 2018-08-06
RU2691210C2 (ru) 2019-06-11
RU2017103099A3 (ru) 2018-12-20
WO2016005031A1 (de) 2016-01-14
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