[go: up one dir, main page]

EP2963369A1 - Method and device for the cryogenic decomposition of air - Google Patents

Method and device for the cryogenic decomposition of air Download PDF

Info

Publication number
EP2963369A1
EP2963369A1 EP15001881.0A EP15001881A EP2963369A1 EP 2963369 A1 EP2963369 A1 EP 2963369A1 EP 15001881 A EP15001881 A EP 15001881A EP 2963369 A1 EP2963369 A1 EP 2963369A1
Authority
EP
European Patent Office
Prior art keywords
air
pressure
air flow
turbine
compressed
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
EP15001881.0A
Other languages
German (de)
French (fr)
Other versions
EP2963369B1 (en
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 PL15001881T priority Critical patent/PL2963369T3/en
Priority to EP15001881.0A priority patent/EP2963369B1/en
Publication of EP2963369A1 publication Critical patent/EP2963369A1/en
Application granted granted Critical
Publication of EP2963369B1 publication Critical patent/EP2963369B1/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

Definitions

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

Landscapes

  • 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 di Vorrichtung dienen zur Tieftemperaturzerlegung von Luft in einer Luftzerlegungsanlage, die einen Hauptluftverdichter, einen Hauptwärmetauscher (8) und ein Destillationssäulen-System mit einer Hochdrucksäule (10) und einer Niederdrucksäule aufweist. Die gesamte Einsatzluft (1) wird in dem Hauptluftverdichter (3) auf einen ersten Luftdruck verdichtet, der mindestens 3 bar höher als der Betriebsdruck der Hochdrucksäule ist. Ein erster Teil des verdichteten Gesamtluftstroms wird als erster Luftstrom (100) unter dem ersten Luftdruck in dem Hauptwärmetauscher (8) abgekühlt und verflüssigt oder pseudo-verflüssigt, anschließend entspannt (101) und in das Destillationssäulen-System eingeleitet (102, 9). Ein zweiter Teil des verdichteten Gesamtluftstroms wird als zweiter Luftstrom (200) in einem turbinengetriebenen Nachverdichter (202c) auf einen zweiten Luftdruck nachverdichtet . Ein erster Teilstrom des zweiten Luftstroms wird als dritter Luftstrom (210) unter dem zweiten Luftdruck und unter einer ersten Temperatur (T1) in eine erste Turbine (202t) eingeleitet, dort arbeitsleistend entspannt und anschließend in das Destillationssäulen-System eingeleitet (211, 213, 22), wobei die erste Turbine (202t) den ersten turbinengetriebenen Nachverdichter (202c) antreibt. Mindestens zeitweise wird mindestens ein Flüssigprodukt (30; 39; LAR) in dem Destillationssäulen-System gewonnen und aus der Luftzerlegungsanlage abgezogen. Ein erster Produktstrom (37; 43) wird flüssig aus dem Destillationssäulen-System abgezogen, in flüssigem Zustand auf einen ersten erhöhten Produktdruck gebracht (41; 44), in dem Hauptwärmetauscher (8) verdampft oder pseudo-verdampft und angewärmt und anschließend als erstes Druckgasprodukt gewonnen. Mindestens zeitweise wird ein zweiter Teilstrom des zweiten Luftstroms als vierter Luftstrom (230) in dem Hauptwärmetauscher (8) in einem Kaltverdichter (14c) auf einen dritten Luftdruck weiterverdichtet, in dem Hauptwärmetauscher (8) abgekühlt und verflüssigt oder pseudo-verflüssigt, anschließend entspannt (233) und in das Destillationssäulen-System eingeleitet (234, 9). Der vierte Luftstrom (230), der durch den Kaltverdichter (14c) strömt, mindestens eine der folgenden Eigenschaften aufweist: - seine Menge ist im zweiten Betriebsmodus größer als im zweiten Betriebsmodus - sein Druck am Austritt des Kaltverdichters ist im zweiten Betriebsmodus höher als im ersten Betriebsmodus.The method and apparatus are for cryogenic separation of air in an air separation plant having a main air compressor, a main heat exchanger (8) and a distillation column system with a high pressure column (10) and a low pressure column. The total feed air (1) is compressed in the main air compressor (3) to a first air pressure which is at least 3 bar higher than the operating pressure of the high-pressure column. A first portion of the total compressed air stream is cooled and liquefied or pseudo-liquefied as the first air stream (100) below the first air pressure in the main heat exchanger (8), then decompressed (101) and introduced into the distillation column system (102, 9). A second part of the compressed total air flow is recompressed as a second air flow (200) in a turbine-driven secondary compressor (202c) to a second air pressure. A first partial flow of the second air flow is introduced as the third air flow (210) under the second air pressure and at a first temperature (T1) into a first turbine (202t), where it works to reduce pressure and then introduced into the distillation column system (211, 213, 22), wherein the first turbine (202t) drives the first turbine-driven boost compressor (202c). At least temporarily, at least one liquid product (30; 39; LAR) is recovered in the distillation column system and withdrawn from the air separation plant. A first product stream (37; 43) is withdrawn liquid from the distillation column system, brought to a first elevated product pressure (41; 44) in the liquid state, vaporized or pseudo-vaporized and heated in the main heat exchanger (8) and then as a first pressurized gas product won. At least temporarily, a second partial stream of the second air stream as the fourth air stream (230) in the main heat exchanger (8) in a cold compressor (14c) further compressed to a third air pressure, cooled in the main heat exchanger (8) and liquefied or pseudo-liquefied, then relaxed ( 233) and introduced into the distillation column system (234, 9). The fourth air stream (230) flowing through the cold compressor (14c) has at least one of the following properties: its quantity is greater in the second operating mode than in the second operating mode - Its pressure at the outlet of the cold compressor is higher in the second operating mode than in the first operating mode.

Description

Die Erfindung betrifft ein Verfahren zur Tieftemperaturzerlegung von Luft, bei dem sowohl mindestens ein Flüssigprodukt als auch mindestens ein innenverdichtetes Produkt gewonnen wird, wobei zwei Luftturbinen eingesetzt werden, die zwei Nachverdichter antreiben, von denen einer als Kaltverdichter ausgebildet ist. Ein derartiges Verfahren ist aus US 2009078001 A1 bekannt.The invention relates to a method for the cryogenic separation of air, in which both at least one liquid product and at least one internally compressed product is obtained, wherein two air turbines are used, driving two booster, one of which is designed as a cold compressor. Such a procedure is over US 2009078001 A1 known.

Unter einem "Hauptluftverdichter" wird hier eine mehrstufige Maschine verstanden, deren Stufen einen gemeinsamen Antrieb (Elektromotor, Dampfturbine oder Gasturbine) aufweisen und in einem gemeinsamen Gehäuse angeordnet sind. Er kann zum Beispiel durch einen Getriebeverdichter gebildet werden, bei welchem die Stufen um das Getriebegehäuse herum gruppiert sind. Dieses Getriebe besitzt ein Großrad welches mehrere parallele Ritzelwellen mit jeweils einer oder zwei Stufen antreibt.A "main air compressor" is here understood to mean a multi-stage machine whose stages have a common drive (electric motor, steam turbine or gas turbine) and are arranged in a common housing. It may be formed, for example, by a gear compressor in which the steps are grouped around the transmission housing. This transmission has a large gear which drives several parallel pinion shafts with one or two stages each.

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 der Erfindung kann als Zwei-Säulen-System (zum Beispiel als klassisches Linde-Doppelsäulensystem), oder auch als Drei- oder Mehr-Säulen-System. Es kann zusätzlich zu den Kolonnen zur Stickstoff-Sauerstoff-Trennung weitere Vorrichtungen zur Gewinnung hochreiner Produkte und/oder anderer Luftkomponenten, insbesondere von Edelgasen aufweisen, beispielsweise eine Argongewinnung und/oder eine Krypton-Xenon-Gewinnung.The distillation column system of the invention can be used as a two-column system (for example, as a classic Linde double column system), or as a three or more column system. It may in addition to the columns for nitrogen-oxygen separation, further devices for obtaining high purity products and / or other air components, in particular of noble gases, for example, an argon production and / or a krypton-xenon recovery.

Bei dem Prozess wird ein flüssig auf Druck gebrachter erster Produktstrom im Hauptwärmetauscher verdampft und schließlich als gasförmiges Druckprodukt gewonnen. Diese Methode wird auch als Innenverdichtung bezeichnet. Für den Fall eines überkritischen Drucks findet kein Phasenübergang im eigentlichen Sinne statt, der Produktstrom wird dann "pseudo-verdampft".In the process, a first product stream which has been brought to liquid pressure is vaporized in the main heat exchanger and finally recovered as a gaseous pressure product. This method is also called internal compression. In the case of a supercritical pressure, no phase transition takes place in the true sense, the product stream is then "pseudo-evaporated".

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 insbesondere durch den ersten und den vierten Luftstrom.Against the (pseudo) evaporating product stream, a high-pressure heat carrier is liquefied (or pseudo-liquefied when it is under supercritical pressure). The heat carrier is often formed by a part of the air, in the present case in particular by the first and the fourth air flow.

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 102008016355 A1 .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 102008016355 A1 ,

In dieser Anmeldung werden mehrfach Prozessparameter wie Mengenströme oder Drücke beschrieben, die in einem Betriebsmodus "kleiner" oder "größer" als in einem anderen Betriebsmodus sind. Damit sind hier gezielte Veränderungen des entsprechenden Parameters durch Regel- und/oder Stelleinrichtungen gemeint und nicht natürliche Schwankungen innerhalb eines stationären Betriebszustands. Diese gezielten Veränderungen können direkt durch Einstellung des Parameters selbst bewirkt werden oder indirekt durch Einstellung anderer Parameter, die Einfluss auf den zu verändernden Parameter haben. Insbesondere ist ein Parameter dann "größer" beziehungsweise "kleiner", wenn der Unterschied zwischen den Mittelwerten des Parameters in den verschiedenen Betriebsmodi mehr als 2 %, insbesondere mehr als 5 %, insbesondere mehr als 10 % beträgt.In this application, multiple process parameters such as mass flows or pressures are described which are "smaller" or "greater" in one operating mode than in another operating mode. This means targeted changes of the corresponding parameter by regulating and / or adjusting devices and not natural fluctuations within a stationary operating state. These targeted changes can be effected directly by adjusting the parameter itself or indirectly by setting other parameters that affect the have to be changed parameters. In particular, a parameter is "larger" or "smaller" if the difference between the mean values of the parameter in the different operating modes is more than 2%, in particular more than 5%, in particular more than 10%.

Bei den Druckangaben werden hier die natürlichen Druckverluste in der Regel nicht einbezogen. Drücke werden hier als "gleich" gewertet, wenn der Druckunterschied zwischen den entsprechenden Stellen nicht größer als die natürlichen Leitungsverluste sind, die durch Druckverluste in Rohrleitungen, Wärmetauschern, Kühlern, Adsorbern etc. verursacht werden. Zum Beispiel erfährt der erste Produktstrom einen Druckverlust in den Passagen des Hauptwärmetauschers; trotzdem werden hier der Abgabedruck des Druckgasprodukts stromabwärts des Hauptwärmetauschers und der Druck stromaufwärts des Hauptwärmetauschers gleichermaßen als "der erste Produktdruck" bezeichnet. Umgekehrt ist der zweite Druck eines Stroms stromabwärts gewisser Verfahrensschritte nur dann "niedriger" oder "höher" als der erste Druck stromaufwärts dieser Schritte, wenn die entsprechende Druckdifferenz höher als die natürlichen Leitungsverluste ist, also insbesondere die Druckerhöhung durch mindestens eine Verdichterstufe beziehungsweise die Druckverminderung gezielt durch mindestens ein Drosselventil und/oder mindestens eine Entspannungsmaschine (Expansionsturbine) erfolgt.In the pressure data, the natural pressure losses are usually not included here. Here, pressures are considered "equal" if the pressure difference between the corresponding points is not greater than the natural conduction losses caused by pressure losses in piping, heat exchangers, coolers, adsorbers, etc. For example, the first product stream experiences a pressure loss in the passages of the main heat exchanger; nevertheless, here the discharge pressure of the compressed gas product downstream of the main heat exchanger and the pressure upstream of the main heat exchanger are referred to equally as "the first product pressure". Conversely, the second pressure of a stream downstream of certain process steps is only "lower" or "higher" than the first pressure upstream of these steps, if the corresponding pressure difference is higher than the natural line losses, ie in particular targeted pressure increase by at least one compressor stage or the pressure reduction by at least one throttle valve and / or at least one expansion machine (expansion turbine) takes place.

Der "Hauptwärmetauscher" dient zur Abkühlung von Einsatzluft in indirektem Wärmeaustausch mit Rückströmen aus dem Destillationssäulen-System. Er kann aus einem einzelnen oder mehreren parallel und/oder seriell verbundenen Wärmetauscherabschnitten gebildet sein, zum Beispiel aus einem oder mehreren Plattenwärmetauscher-Blöcken.The "main heat exchanger" serves to cool feed air in indirect heat exchange with reflux streams from the distillation column system. It may be formed from a single or multiple parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art und eine Vorrichtung anzugeben, die mit stark variierendem Flüssigproduktanteil gefahren werden kann. Zum "Flüssigproduktanteil" zählen dabei nur Ströme, welche die Luftzerlegungsanlage flüssig verlassen und beispielsweise in einen Flüssigtank eingeleitet werden, nicht aber innenverdichtete Ströme, die zwar dem Destillationssäulen-System flüssig entnommen, aber innerhalb der Luftzerlegungsanlage verdampft oder pseudo-verdampft und schließlich in gasförmigem Zustand aus der Luftzerlegungsanlage herausgeführt werden.The invention has for its object to provide a method of the type mentioned above and a device that can be driven with greatly varying liquid product content. The "liquid product content" include only streams that leave the air separation plant liquid and introduced, for example, in a liquid tank, but not internally compressed streams, although taken from the distillation column system liquid, but vaporized within the air separation plant or pseudo-evaporated and finally in a gaseous state be led out of the air separation plant.

Diese Aufgabe wird durch die Merkmale des Patentanspruchs 1 gelöst.This object is solved by the features of patent claim 1.

Bei der Erfindung ist der "erste Betriebsmodus" für eine besonders hohe Flüssigproduktion, insbesondere für maximale Flüssigproduktion (Gesamtmenge an Flüssigprodukten, die aus der Luftzerlegungsanlage abgezogen wird) ausgelegt. Der "zweite Betriebsmodus" ist demgegenüber für einen geringeren Flüssigproduktanteil ausgelegt, der zum Beispiel auch null sein kann (reiner Gasbetrieb). Die Gesamtmenge an Flüssigprodukten beträgt im zweiten Betriebsmodus beispielsweise 0 %, oder liegt etwas höher, zum Beispiel zwischen 50% und 100% der maximalen Flüssigproduktmenge. (Alle Prozentangaben beziehen sich hier und im Folgenden auf die molare Menge, soweit nichts anderes angegeben ist. Die molare Menge kann beispielsweise in Nm3/h angegeben werden.)In the invention, the "first mode of operation" is designed for a particularly high liquid production, in particular for maximum liquid production (total amount of liquid products withdrawn from the air separation plant). By contrast, the "second operating mode" is designed for a lower proportion of liquid product, which may also be zero, for example (pure gas operation). For example, the total amount of liquid products in the second mode of operation is 0%, or slightly higher, for example, between 50% and 100% of the maximum liquid product amount. (All percentages here and below refer to the molar amount, unless stated otherwise.) The molar amount can be given in Nm 3 / h, for example.)

Bei dem erfindungsgemäßen Verfahren wird ein turbinengetriebener Kaltverdichter eingesetzt, der im ersten Betriebsmodus mit niedrigerer Last gefahren wird als im zweiten. Es erscheint auf den ersten Blick nicht zielführend, in dem Betrieb mit maximaler Flüssigproduktion Turbinen mit weniger Durchsatz zu betreiben, da Turbinen grundsätzlich zur Produktion der Kälte für die Produktverflüssigung eingesetzt werden können. Im Rahmen der Erfindung hat es sich jedoch herausgestellt, dass durch diese Maßnahme eine besonders starke Variation der Flüssigproduktmenge möglich ist, wobei in beiden Betriebsmodi ein zufriedenstellender Wirkungsgrad erreicht wird, also insgesamt ein vergleichsweise geringer Energieverbrauch.In the method according to the invention, a turbine-driven cold compressor is used, which is operated in the first operating mode with a lower load than in the second. At first glance, it does not appear expedient to operate turbines with a lower throughput in the operation with maximum liquid production since turbines can generally be used to produce the refrigeration for the product liquefaction. In the context of the invention, however, it has been found that by this measure, a particularly large variation of the liquid product amount is possible, with a satisfactory efficiency is achieved in both operating modes, so a comparatively low energy consumption.

Unter einem "Kaltverdichter" wird hier ein Verdichtungsorgan verstanden, bei dem das Gas der Verdichtung bei einer Temperatur zugeführt wird, die deutlich unterhalb der Umgebungstemperatur liegt, im allgemeinen unterhalb von 250 K, vorzugsweise unterhalb von 200 K.A "cold compressor" is here understood to mean a compression member in which the gas is supplied to the compression at a temperature which is significantly below the ambient temperature, generally below 250 K, preferably below 200 K.

Der Kaltverdichter kann bei dem erfindungsgemäßen Verfahren durch einen Elektromotor angetrieben werden. In vielen Fällen ist es jedoch günstig, eine Turbinen-Kaltverdichter-Kombination einzusetzen, wie es im Patentanspruch 2 beschrieben ist. Die Luftmenge, die als fünfter Luftstrom durch die zweite Turbine geht, die den Kaltverdichter antreibt, ist in dem ersten Betriebsmodus geringer als im zweiten Betriebsmodus. In einem extremen Beispiel ist die Turbinen-Kaltverdichter-Kombination im ersten Betriebsmodus vollständig außer Betrieb, also die entsprechende Luftmenge gleich Null.The cold compressor can be driven by an electric motor in the inventive method. In many cases, however, it is favorable to use a turbine-cold compressor combination, as described in claim 2. The amount of air passing through the second turbine as the fifth airflow that drives the cold compressor is less in the first mode of operation than in the second mode of operation. In an extreme example, the turbine-cold compressor combination completely out of operation in the first operating mode, ie the corresponding amount of air equal to zero.

Der Eintrittsdruck der zweiten Turbine kann etwa gleich dem Eintrittsdruck der ersten Turbine sein; vorzugsweise sind die beiden Eintrittsdrücke aber verschieden. Insbesondere kann der Eintrittsdruck der zweiten Turbine niedriger als derjenige der ersten Turbine sein und zum Beispiel gleich dem ersten Luftdruck sein.The inlet pressure of the second turbine may be approximately equal to the inlet pressure of the first turbine; Preferably, however, the two inlet pressures are different. In particular, the inlet pressure of the second turbine may be lower than that of the first turbine and, for example, equal to the first air pressure.

Es ist günstig, wenn im ersten Betriebsmodus nur ein relativ kleiner Teil der Einsatzluft auf den dritten, höheren Luftdruck verdichtet wird, wie es in Patentanspruch 3 beschrieben wird. Der dritte Luftdruck kann außerdem im zweiten Betriebsmodus höher liegen als beim ersten Betriebsmodus.It is favorable if, in the first operating mode, only a relatively small part of the feed air is compressed to the third, higher air pressure, as described in patent claim 3. The third air pressure may also be higher in the second operating mode than in the first operating mode.

In einer besonders bevorzugten Ausführungsform wird der dritte Luftstrom in der ersten Turbine auf einen Austrittsdruck entspannt wird, der gleich dem Betriebsdruck der Hochdrucksäule (plus Leitungsverlusten) ist.In a particularly preferred embodiment, the third air flow in the first turbine is relieved to an outlet pressure equal to the operating pressure of the high pressure column (plus line losses).

Der Austrittsdruck der zweiten Turbine kann ebenfalls gleich dem Betriebsdruck der Hochdrucksäule (plus Leitungsverlusten) sein oder auch niedriger liegen, zum Beispiel beim Betriebsdruck der Niederdrucksäule (plus Leitungsverlusten), siehe Patentansprüche 5 und 6. Der dritte Teilstrom wird dann beispielsweise in die Niederdrucksäule eingeleitet.The outlet pressure of the second turbine can also be equal to the operating pressure of the high pressure column (plus line losses) or lower, for example, the operating pressure of the low pressure column (plus line losses), see claims 5 and 6. The third partial flow is then introduced, for example in the low pressure column.

Ansonsten können die entspannten Teilströme zum Teil oder vollständig in die Hochdrucksäule eingeleitet werden, wie es die Patentansprüche 7 und 8 erläutern.Otherwise, the relaxed partial flows can be introduced partially or completely into the high-pressure column, as explained in the claims 7 and 8.

Wie in Patentanspruch 9 erläutert, kann in Verfahren mehr als ein Innenverdichtungsprodukt erzeugt werden, auch mehr als zwei Innenverdichtungsprodukte. Die verschiedenen Innenverdichtungsprodukte können sich in ihrer chemischen Zusammensetzung unterschieden (zum Beispiel Sauerstoff/Stickstoff oder auch Sauerstoff oder Stickstoff verschiedener Reinheit) oder in ihrem Druck oder in beidem.As explained in claim 9, more than one internal compaction product can be produced in processes, including more than two interior compaction products. The different internal compaction products may differ in their chemical composition (for example, oxygen / nitrogen or else oxygen or nitrogen of different purity) or in their pressure or both.

Die Erfindung betrifft außerdem eine Luftzerlegungsanlage in Form einer Vorrichtung gemäß Patentanspruch 10. Die erfindungsgemäße Vorrichtung kann durch Vorrichtungsmerkmale ergänzt werden, die den Merkmalen der abhängigen Verfahrensansprüche entsprechen.The invention also relates to an air separation plant in the form of a device according to claim 10. The inventive device can by Device features are added, which correspond to the features of the dependent method claims.

Bei den "Mitteln zum Umschalten zwischen einem ersten und einem zweiten Betriebsmodus" handelt es sich um komplexe Regel- und Steuerungsvorrichtungen, die im Zusammenwirken ein mindestens teilweise automatisches Umschalten zwischen den beiden Betriebsmodi ermöglichen, beispielsweise um ein entsprechend programmiertes Betriebsleitsystem.The "means for switching between a first and a second operating mode" are complex control and control devices, which allow in cooperation at least partially automatic switching between the two operating modes, for example, a correspondingly programmed operation control system.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand eines in der Zeichnung schematisch dargestellten Ausführungsbeispiels näher erläutert.The invention and further details of the invention are explained in more detail below with reference to an embodiment schematically illustrated in the drawing.

Das Ausführungsbeispiel der Erfindung wird im Folgenden zunächst anhand des ersten Betriebsmodus erläutert, der hier auf maximale Flüssigproduktion ausgelegt ist. Atmosphärische Luft 1 (AIR) wird über ein Filter 2 von einem Hauptluftverdichter 3 angesaugt und auf einen ersten Luftdruck von beispielsweise 22 bar verdichtet. Stromabwärts des Hauptluftverdichters 3 wird die verdichtete Gesamtluft 4 unter dem ersten Luftdruck in einer Vorkühleinrichtung 5 und anschließend in einer Reinigungseinrichtung 6 behandelt. Die gereinigte Gesamtluft 7 wird in einen ersten Luftstrom 100 und einen zweiten Luftstrom 200 aufgeteilt.The embodiment of the invention is first explained below with reference to the first operating mode, which is designed here for maximum liquid production. Atmospheric air 1 (AIR) is sucked in via a filter 2 from a main air compressor 3 and compressed to a first air pressure of, for example, 22 bar. Downstream of the main air compressor 3, the compressed total air 4 is treated under the first air pressure in a precooling device 5 and subsequently in a cleaning device 6. The purified total air 7 is divided into a first air flow 100 and a second air flow 200.

Der erste Luftstrom 100 wird in einem Hauptwärmetauscher 8 vom warmen bis zum kalten Ende abgekühlt und dabei (pseudo-)verflüssigt und anschließend in einem Drosselventil 101 auf etwa den Betriebsdruck der später erläuterten Hochdrucksäule entspannt, der vorzugsweise 5 bar bis 7 bar, beispielsweise 6 bar beträgt. Der entspannte erste Luftstrom 102 wird über Leitung 9 dem Destillationssäulen-System zugeführt, das eine Hochdrucksäule 10, einen Hauptkondensator 11, der als Kondensator-Verdampfer ausgebildet ist, und eine Niederdrucksäule 12 aufweist.The first air stream 100 is cooled in a main heat exchanger 8 from the hot to the cold end and (pseudo-) liquefied and then expanded in a throttle valve 101 to about the operating pressure of the later described high-pressure column, preferably 5 bar to 7 bar, for example 6 bar is. The expanded first air stream 102 is fed via line 9 to the distillation column system, which has a high-pressure column 10, a main condenser 11, which is designed as a condenser-evaporator, and a low-pressure column 12.

Der zweite Luftstrom 200 wird in einem ersten turbinengetriebenen Nachverdichter 202c mit Nachkühler 203 auf einen zweiten Luftdruck von beispielsweise 28 bar nachverdichtet. Der riachverdichtete zweite Luftstrom 204 wird in einen dritten Luftstrom 210 und einen vierten Luftstrom 230 aufgeteilt.The second air stream 200 is recompressed in a first turbine-driven secondary compressor 202c with aftercooler 203 to a second air pressure of, for example, 28 bar. The riachverdichtet second air stream 204 is divided into a third air flow 210 and a fourth air flow 230.

Der dritte Luftstrom 210 wird dem Hauptwärmetauscher 8 am warmen Ende zugeführt und bei einer ersten Zwischentemperatur T1 wieder entnommen. Unter dieser Zwischentemperatur und dem zweiten Luftdruck wird der dritte Luftstrom einer ersten Turbine 202t zugeführt und dort arbeitsleistend auf den Betriebsdruck der Hochdrucksäule 10 entspannt, der 5 bar bis 7 bar, beispielweise 6 bar beträgt. Die erste Turbine 202t ist mechanisch mit dem ersten Nachverdichter 202c gekoppelt. Der arbeitsleistend entspannte dritte Luftstrom 211 wird in einem Abscheider (Phasentrenner) 212 eingeleitet und dort von einem geringen Flüssiganteil befreit. Anschließend strömt er rein gasförmig über die Leitungen 213 und 13 zum Sumpf der Hochdrucksäule 10. Der Turbineneintrittsdruck ist hier gleich dem zweiten Luftdruck.The third air flow 210 is supplied to the main heat exchanger 8 at the warm end and removed again at a first intermediate temperature T1. Under this intermediate temperature and the second air pressure of the third air flow of a first turbine 202 t is supplied and there work to relax the operating pressure of the high-pressure column 10, which is 5 bar to 7 bar, for example, 6 bar. The first turbine 202t is mechanically coupled to the first boost compressor 202c. The working expanded third air stream 211 is introduced into a separator (phase separator) 212 and there freed of a small proportion of liquid. It then flows in pure gaseous form via the lines 213 and 13 to the sump of the high-pressure column 10. The turbine inlet pressure here is equal to the second air pressure.

In dem Destillationssäulen-System wird die Sumpfflüssigkeit 15 der Hochdrucksäule in einem Unterkühlungs-Gegenströmer 16 abgekühlt und über Leitung 17 einem Argonteil 500 zugeleitet, der später erläutert wird. Von dort tritt sie zum Teil flüssig (Leitung 18) und zum Teil gasförmig (Leitung 19) inter Niederdrucksäulendruck wieder aus und wird an geeigneter Stelle in die Niederdrucksäule 12 eingespeist. (Falls kein Argonteil vorhanden ist, wird die unterkühlte Sumpfflüssigkeit unmittelbar auf Niederdrucksäulendruck entspannt und in die Niederdrucksäule eingeleitet.)In the distillation column system, the bottom liquid 15 of the high pressure column is cooled in a subcooling countercurrent 16 and fed via line 17 to an argon part 500 which will be explained later. From there it exits in part liquid (line 18) and partly gaseous (line 19) inter low pressure column pressure again and is fed at a suitable location in the low-pressure column 12. (If no argon portion is present, the supercooled bottom liquid is immediately depressurized to low pressure column pressure and introduced into the low pressure column.)

Mindestens ein Teil der über Leitung 9 in die Hochdrucksäule 10 geleiteten Flüssigluft wird über Leitung 18 wieder entnommen, ebenfalls im Unterkühlungs-Gegenströmer 16 abgekühlt und über Ventil 21 und Leitung 22 der Niederdrucksäule 12 zugeführt.At least a portion of the guided via line 9 in the high pressure column 10 liquid air is removed again via line 18, also cooled in the subcooling countercurrent 16 and fed via valve 21 and line 22 of the low pressure column 12.

Der gasförmige Kopfstickstoff 23 der Hochdrucksäule 10 wird zu einem ersten Teil 24 in den Verflüssigungsraum des Hauptkondensators 11 eingeleitet und dort im Wesentlichen vollständig verflüssigt. Der dabei gewonnene Flüssigstickstoff 25 wird zu einem ersten Teil 26 als Rücklauf auf die Hochdrucksäule 10 aufgegeben. Ein zweiter Teil 27 wird im Unterkühlungs-Gegenströmer 16 abgekühlt und über Ventil 28 und Leitung der Niederdrucksäule 12 am Kopf zugeführt. Ein Teil davon wird im ersten Betriebsmodus über Leitung 30 wieder entnommen und als Flüssigstickstoffprodukt (LIN) gewonnen und aus der Luftzerlegungsanlage abgezogen.The gaseous top nitrogen 23 of the high-pressure column 10 is introduced to a first part 24 in the liquefaction space of the main condenser 11 and there substantially completely liquefied. The liquid nitrogen 25 obtained in the process is fed to a first part 26 as reflux to the high-pressure column 10. A second part 27 is cooled in the subcooling countercurrent 16 and fed via valve 28 and line of the low pressure column 12 at the top. Part of it is removed again in the first operating mode via line 30 and recovered as liquid nitrogen product (LIN) and withdrawn from the air separation plant.

Vom Kopf der Niederdrucksäule, in dem ein Druck von 1,2 bar bis 1,6 bar, beispielweise 1,3 bar herrscht, wird gasförmiger Niederdruckstickstoff 31 entnommen, im Unterkühlungs-Gegenströmer 16 und im Hauptwärmetauscher 8 angewärmt und über Leitung 32 als gasförmiges Niederdruckprodukt (GAN) abgezogen. Gasförmiger Unreinstickstoff 33 aus der Niederdrucksäule wird ebenfalls in Unterkühlungs-Gegenströmer 16 und Hauptwärmetauscher 8 angewärmt. Der warme Unreinstickstoff 34 kann entweder über Leitung 35 in die Atmosphäre (ATM) abgeblasen oder über Leitung 36 als Regeneriergas in der Reinigungseinrichtung 6 eingesetzt werden.From the top of the low-pressure column, in which a pressure of 1.2 bar to 1.6 bar, for example 1.3 bar prevails, gaseous low-pressure nitrogen 31 is removed, heated in the supercooling countercurrent 16 and in the main heat exchanger 8 and withdrawn via line 32 as a gaseous low pressure product (GAN). Gaseous impure nitrogen 33 from the low-pressure column is also warmed in supercooling countercurrent 16 and main heat exchanger 8. The warm impure nitrogen 34 can either be blown off via line 35 into the atmosphere (ATM) or be used via line 36 as a regeneration gas in the cleaning device 6.

Vom Sumpf der Niederdrucksäule 12 (genau genommen aus dem Verdampfungsraum des Hauptkondensators 11) wird über Leitung 37 flüssiger Sauerstoff abgezogen. Ein erster Teil 38 wird gegebenenfalls im Unterkühlungs-Gegenströmer 16 unterkühlt und über Leitung 39 als Flüssigsauerstoffprodukt (GOX) gewonnen und aus der Luftzerlegungsanlage abgezogen. Ein zweiter Teil 40 bildet den "ersten Produktstrom", wird in einer Pumpe 41 auf einen ersten Produkt von beispielsweise 37 bar gebracht, unter diesem hohen Druck in dem Hauptwärmetauscher 16 verdampft und auf etwa Umgebungstemperatur angewärmt. Der warme Drucksauerstoff 42 wird als sauerstoffreiches erstes Druckgasprodukt (GOX IC) abgegeben.From the bottom of the low-pressure column 12 (strictly speaking, from the evaporation space of the main condenser 11), liquid oxygen is withdrawn via line 37. A first part 38 is optionally supercooled in the supercooling countercurrent 16 and recovered via line 39 as a liquid oxygen product (GOX) and withdrawn from the air separation plant. A second part 40 forms the "first product stream" is brought in a pump 41 to a first product, for example, 37 bar, evaporated under this high pressure in the main heat exchanger 16 and warmed to about ambient temperature. The warm pressure oxygen 42 is released as an oxygen-rich first compressed gas product (GOX IC).

Ein weiteres Innenverdichtungsprodukt kann aus einem dritten Teil 43 des flüssigen Stickstoffs 25 aus dem Hauptkondensator 11 gewonnen werden. Dieser wird als "zweiter Produktstrom" in einer Pumpe 44 flüssig auf einen zweiten Produktdruck von beispielsweise auch 37 bar gebracht. Unter diesem zweiten Produktdruck wird er im Hauptwärmetauscher 8 verdampft und auf etwa Umgebungstemperatur angewärmt. Der warme Druckstickstoff 45 wird schließlich unter dem zweiten Produktdruck als stickstoffreiches Druckgasprodukt (GAN IC) abgegeben.Another interior compression product may be recovered from a third portion 43 of the liquid nitrogen 25 from the main condenser 11. This is brought as a "second product stream" in a pump 44 liquid to a second product pressure of, for example, 37 bar. Under this second product pressure, it is vaporized in the main heat exchanger 8 and warmed to about ambient temperature. The warm pressure nitrogen 45 is finally released under the second product pressure as a nitrogen-rich compressed gas product (GAN IC).

Ein dritter Teil 230 des zweiten Luftstroms 204 bildet einen "vierten Luftstrom"; dieser wird in dem Hauptwärmetauscher (8) auf eine erste Zwischentemperatur (T3) abgekühlt, in einem Kaltverdichter (14c) auf einen dritten Luftdruck von beispielsweise 40 bar weiterverdichtet und durchströmt unter diesem sehr hohen Druck den Hauptwärmetauscher bis zum kalten Ende. Der kalte pseudo-verflüssigte dritte Teil 232 wird in einem Drosselventil 233 auf Hochdrucksäulendruck entspannt und über die Leitungen 234 und 9 der Hochdrucksäule 10 zugeführt.A third part 230 of the second air flow 204 forms a "fourth air flow"; this is cooled in the main heat exchanger (8) to a first intermediate temperature (T3), further compressed in a cold compressor (14c) to a third air pressure of, for example, 40 bar and flows through the main heat exchanger up to the cold end under this very high pressure. The cold pseudo-liquefied third part 232 is expanded in a throttle valve 233 to high-pressure column pressure and fed via the lines 234 and 9 of the high-pressure column 10.

Der Kaltverdichter 14c wird von einer zweiten Expansionsturbine 14t angetrieben, in der ein dritter Teilstrom 301 des verdichteten Gesamtluftstroms 7 als "fünfter Luftstrom" arbeitsleistend entspannt wird von dem ersten Luftdruck auf den Betriebsdruck der Hochdrucksäule 10. Die zweite Turbine weist eine Eintrittstemperatur T2 auf. Der arbeitsleistend entspannte fünfte Luftstrom 302 wird über Leitung 13 in die Hochdrucksäule 10 eingeleitet.The cold compressor 14c is driven by a second expansion turbine 14t, in which a third partial flow 301 of the compressed total air flow 7 as a "fifth air flow" is released from the first air pressure to the operating pressure High pressure column 10. The second turbine has an inlet temperature T2. The working expanded fifth air flow 302 is introduced via line 13 into the high-pressure column 10.

Abweichend von dem hier dargestellten Ausführungsbeispiel können die beiden Turbineneintrittstemperaturen T1 und T2 im Rahmen der Erfindung auch gleich sein.Notwithstanding the embodiment shown here, the two turbine inlet temperatures T1 and T2 may be the same in the invention.

Falls ein Argonprodukt benötigt wird, weist die Luftzerlegungsanlage außerdem einen Argonteil 500 auf, der wie in EP 2447563 A1 beschrieben funktioniert und ein weiteres Flüssigprodukt in Form flüssigen Reinargons (LAR) produziert, das über Leitung 501 abgezogen wird.If an argon product is needed, the air separation plant also includes an argon part 500 which, as in FIG EP 2447563 A1 described and produces another liquid product in the form of liquid pure argon (LAR), which is withdrawn via line 501.

Die "erste Gesamtmenge an Flüssigprodukten", die in einem ersten Betriebsmodus aus der Luftzerlegungsanlage abgezogen wird, setzt sich bei diesem Ausführungsbeispiel aus den Strömen 30 (LIN), 39 (LOX) und 501 (LAR) zusammen. In dem ersten Betriebsmodus liegt das Verhältnis der Gesamtmenge an Flüssigprodukten (LOX, LIN, LAR) zu der Menge an sauerstoffreichem Druckgasprodukt 42 (GOX IC, "erstes Druckgasprodukt") zwischen 20 und 30 %. Die Leistung der Turbine 14t beträgt weniger als 20 % der Leistung der Turbine 202t.The "first total quantity of liquid products", which is withdrawn from the air separation plant in a first operating mode, in this exemplary embodiment is composed of the streams 30 (LIN), 39 (LOX) and 501 (LAR). In the first operating mode, the ratio of the total amount of liquid products (LOX, LIN, LAR) to the amount of oxygen-rich compressed gas product 42 (GOX IC, "first compressed gas product") is between 20 and 30%. The turbine 14t power is less than 20% of the power of the turbine 202t.

In einem zweiten Betriebsmodus wird die Anlage mit einer geringeren "zweiten Gesamtmenge an Flüssigprodukten" und geringerem Verhältnis der Gesamtmenge an Flüssigprodukten (LOX, LIN, LAR) zu der Menge an sauerstoffreichem Druckgasprodukt 42 (GOX IC, "erstes Druckgasprodukt") gefahren. In der Regel wird die Strömungsmenge in mindestens einer der Leitungen 30 und 39 reduziert, vorzugsweise in beiden. Die Argon-Produktion wird in der Regel nicht gezielt gedrosselt, da in meisten Fallen die maximale Argon-Ausbeute gewünscht ist. Auch die Mengen und Drücke der Innenverdichtungsprodukte 42, 45 bleiben konstant.In a second mode of operation, the plant is run with a lower "second total amount of liquid products" and lower ratio of total liquid products (LOX, LIN, LAR) to the amount of oxygen-rich pressurized gas product 42 (GOX IC, "first pressurized gas product"). In general, the flow rate is reduced in at least one of the lines 30 and 39, preferably in both. The argon production is usually not targeted throttled, since in most cases the maximum argon yield is desired. Also, the amounts and pressures of the internal compression products 42, 45 remain constant.

Im zweiten Betriebsmodus werden die Turbinenleistungen verschoben, die Turbine 14t wird hochgefahren, insbesondere auf Voillast und die Leistung der Turbine 202t wird reduziert. Das Verhältnis der Leistungen der Turbinen 14t/202t beträgt beispielsweise weniger als 30%In the second mode of operation, the turbine powers are shifted, the turbine 14t is ramped up, in particular to Voillast and the power of the turbine 202t is reduced. For example, the ratio of turbine 14t / 202t power is less than 30%

Außerdem werden die Gesamtluftmenge und der Enddruck des Verdichters reduziert, sodass der Hauptluftverdichter 3 weniger Energie verbraucht. Der Innenverdichtungsprozess wird aber dadurch verbessert, dass der vierte und der fünfte Teilstrom 230, 301 erhöht werden und damit mehr Hochdruckluft 232 zur Verfügung steht. Die Luftmenge durch die Leitung 100 wird geringer oder gleich hoch wie im ersten Betriebsmodus. Mit der Verringerung der Flüssigproduktion beim Übergang von den ersten auf den zweiten Betriebsfall wird die Last der zweiten Turbine 14t erhöht und die Last der ersten Turbine 202t vermindert.In addition, the total amount of air and the discharge pressure of the compressor are reduced, so that the main air compressor 3 consumes less energy. However, the internal compression process is improved by increasing the fourth and fifth substream 230, 301 and thus providing more high-pressure air 232. The amount of air through the line 100 is less than or equal to the first operating mode. With the reduction of liquid production in the transition from the first to the second operation case, the load of the second turbine 14t is increased and the load of the first turbine 202t is reduced.

Grundsätzlich kann der beschriebene Prozess zeitweise auch stationär gefahren werden, das heißt mit gleich bleibender Flüssigproduktion. In einem anderen Anwendungsfall kann es sinnvoll sein, die Kombination aus zweiter Turbine 14t und Kaltverdichter 14c im ersten Betriebsmodus ganz stillzulegen.In principle, the described process can also be operated at times in a stationary manner, that is, with constant liquid production. In another application, it may be useful to completely shut down the combination of second turbine 14t and cold compressor 14c in the first operating mode.

Die zweite Turbine 14t kann auch so ausgebildet sein, dass sie nicht in die Hochdrucksäule 10, sondern in die Niederdrucksäule 12 einbläst; durch das entsprechend erhöhte Druckverhältnis kann mehr Energie für den Kaltverdichter zur Verfügung gestellt werden.The second turbine 14t can also be designed so that it does not blow into the high-pressure column 10, but rather into the low-pressure column 12; Due to the correspondingly increased pressure ratio, more energy can be made available for the cold compressor.

Der Effekt der Erfindung kann weiter verstärkt werden, indem dem Kaltverdichter 14c ein abschaltbarer zweiter Kaltverdichter nachgeschaltet ist. Der Strom aus dem ersten Kaltverdichter 14c wird im zweiten Betriebsmodus durch einen zweiten Kaltverdichter geleitet, bevor er wieder in den Hauptwärmetauscher eingeführt wird. Der zweite Kaltverdichter wird mit einem Elektromotor angetrieben. Im ersten Betriebsmodus wird der zweite Kaltverdichter ausgeschaltet und der Strom aus dem ersten Kaltverdichter 14c fließt über eine Bypass-Leitung an dem zweiten Kaltverdichter vorbei.The effect of the invention can be further enhanced by connecting a disconnectable second cold compressor downstream of the cold compressor 14c. The stream from the first cold compressor 14c is passed through a second cold compressor in the second operating mode before it is reintroduced into the main heat exchanger. The second cold compressor is driven by an electric motor. In the first mode of operation, the second cold compressor is switched off and the flow from the first cold compressor 14c flows past the second cold compressor via a bypass line.

Claims (10)

Verfahren zur Tieftemperaturzerlegung von Luft in einer Luftzerlegungsanlage, die einen Hauptluftverdichter, einen Hauptwärmetauscher (8) und ein Destillationssäulen-System mit einer Hochdrucksäule (10) und einer Niederdrucksäule aufweist, wobei - die gesamte Einsatzluft (1) in dem Hauptluftverdichter (3) auf einen ersten Luftdruck verdichtet wird, der mindestens 3 bar höher als der Betriebsdruck der Hochdrucksäule ist, um einen verdichteten Gesamtluftstrom (4, 7) zu bilden, - ein erster Teil des verdichteten Gesamtluftstroms als erster Luftstrom (100) unter dem ersten Luftdruck in dem Hauptwärmetauscher (8) abgekühlt und verflüssigt oder pseudo-verflüssigt, anschließend entspannt (101) und in das Destillationssäulen-System eingeleitet (102, 9) wird, - ein zweiter Teil des verdichteten Gesamtluftstroms als zweiter Luftstrom (200) in einem ersten turbinengetriebenen Nachverdichter (202c) auf einen zweiten Luftdruck nachverdichtet wird, der höher als der erste Luftdruck ist, - ein erster Teilstrom des nachverdichteten zweiten Luftstroms als dritter Luftstrom (210) unter dem zweiten Luftdruck und unter einer ersten Temperatur (T1) in eine erste Turbine (202t) eingeleitet, dort arbeitsleistend entspannt und anschließend in das Destillationssäulen-System eingeleitet (211, 213, 22) wird, wobei die erste Turbine (202t) den ersten turbinengetriebenen Nachverdichter (202c) antreibt, - mindestens zeitweise mindestens ein Flüssigprodukt (30; 39; LAR) in dem Destillationssäulen-System gewonnen und aus der Luftzerlegungsanlage abgezogen wird, - ein erster Produktstrom (37; 43) flüssig aus dem Destillationssäulen-System abgezogen, in flüssigem Zustand auf einen ersten erhöhten Produktdruck gebracht (41; 44), in dem Hauptwärmetauscher (8) verdampft oder pseudo-verdampft und angewärmt wird und - der angewärmte erste Produktstrom (42; 45) als erstes Druckgasprodukt aus der Luftzerlegungsanlage abgezogen wird,
wobei - mindestens zeitweise - ein zweiter Teilstrom des nachverdichteten zweiten Luftstroms als vierter Luftstrom (230) in dem Hauptwärmetauscher (8) auf eine erste Zwischentemperatur (T3) abgekühlt, in einem Kaltverdichter (14c) auf einen dritten Luftdruck weiterverdichtet wird, der höher als der zweite Luftdruck ist und - der weiterverdichtete vierte Luftstrom (231) unter dem dritten Luftdruck in dem Hauptwärmetauscher (8) abgekühlt und verflüssigt oder pseudo-verflüssigt, anschließend entspannt (233) und in das Destillationssäulen-System eingeleitet (234, 9) wird, - in einem ersten Betriebsmodus eine erste Gesamtmenge an Flüssigprodukten (30; 39; LAR) aus der Luftzerlegungsanlage abgezogen wird, - in einem zweiten Betriebsmodus eine zweite Gesamtmenge an Flüssigprodukten (30; 39; LAR) aus der Luftzerlegungsanlage abgezogen wird, die geringer als die erste Gesamtmenge ist, und dass - der vierte Luftstrom (230), der durch den Kaltverdichter (14c) strömt, mindestens eine der folgenden Eigenschaften aufweist: - seine Menge ist im zweiten Betriebsmodus größer als im ersten Betriebsmodus - sein Druck am Austritt des Kaltverdichters ist im zweiten Betriebsmodus höher als im ersten Betriebsmodus. A process for the cryogenic separation of air in an air separation plant comprising a main air compressor, a main heat exchanger (8) and a distillation column system with a high pressure column (10) and a low pressure column, wherein - The total feed air (1) is compressed in the main air compressor (3) to a first air pressure which is at least 3 bar higher than the operating pressure of the high pressure column to form a compressed total air flow (4, 7) a first part of the compressed total air flow is cooled and liquefied or liquefied or pseudo-liquefied as the first air flow (100) under the first air pressure in the main heat exchanger (8), then expanded (101) and introduced into the distillation column system (102, 9), a second part of the compressed total air flow is recompressed as a second air flow (200) in a first turbine-driven secondary compressor (202c) to a second air pressure which is higher than the first air pressure, - A first partial flow of the second secondary air flow as a third air stream (210) under the second air pressure and at a first temperature (T1) in a first turbine (202t) introduced, there worked to reduce work and then introduced into the distillation column system (211, 213 , 22), wherein the first turbine (202t) drives the first turbine-driven booster (202c), at least temporarily at least one liquid product (30; 39; LAR) is recovered in the distillation column system and withdrawn from the air separation plant, a first product stream (37; 43) is withdrawn liquid from the distillation column system, brought to a first elevated product pressure (41; 44) in the liquid state, vaporized or pseudo-evaporated and heated in the main heat exchanger (8) and the heated first product stream (42, 45) is withdrawn from the air separation plant as the first compressed gas product,
in which - at least temporarily - A second partial flow of the second secondary air stream as a fourth air stream (230) in the main heat exchanger (8) to a first Intermediate temperature (T3) cooled in a cold compressor (14c) is further compressed to a third air pressure, which is higher than the second air pressure and the further compressed fourth air stream (231) is cooled below the third air pressure in the main heat exchanger (8) and liquefied or pseudo-liquefied, then expanded (233) and introduced into the distillation column system (234, 9), in a first mode of operation, a first total quantity of liquid products (30, 39, LAR) is withdrawn from the air separation plant, in a second mode of operation, a second total quantity of liquid products (30; 39; LAR) is withdrawn from the air separation plant which is less than the first total amount, and the fourth air stream (230) flowing through the cold compressor (14c) has at least one of the following properties: its quantity is greater in the second operating mode than in the first operating mode - Its pressure at the outlet of the cold compressor is higher in the second operating mode than in the first operating mode. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass - mindestens zeitweise - ein dritter Teil des verdichteten Gesamtluftstroms als fünfter Luftstrom (301) unter dem ersten Luftdruck und bei einer zweiten Temperatur (T2) in eine zweite Turbine (14t) eingeleitet und dort arbeitsleistend entspannt wird, - die zweite Turbine (14t) einen zweiten turbinengetriebenen Nachverdichter antreibt, der durch den Kaltverdichter (14c) gebildet wird, - der arbeitsleistend entspannte fünfte Luftstrom (302) in das Destillationssäulen-System eingeleitet (13) wird und dass - in dem ersten Betriebsmodus die Luftmenge, die als fünfter Luftstrom (301, 302) durch die zweite Turbine (14t) geleitet wird, geringer ist als im zweiten Betriebsmodus. Method according to claim 1, characterized in that - at least temporarily a third part of the compressed total air flow is introduced as the fifth air flow (301) under the first air pressure and at a second temperature (T2) into a second turbine (14t) and is expanded there to perform work, the second turbine (14t) drives a second turbine-driven secondary compressor, which is formed by the cold compressor (14c), - the work-performing relaxed fifth air stream (302) is introduced into the distillation column system (13) and that - In the first mode of operation, the amount of air that is passed as the fifth air flow (301, 302) through the second turbine (14t) is lower than in the second mode of operation. Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass - in dem ersten Betriebsmodus - eine erste Luftmenge des verdichteten Gesamtluftstroms den ersten Luftstrom (100) bildet und - eine zweite Luftmenge des verdichteten Gesamtluftstroms den zweiten Luftstrom (200) bildet
und - in dem zweiten Betriebsmodus - eine dritte Luftmenge des verdichteten Gesamtluftstroms, die gleich oder geringer als die erste Luftmenge ist, den ersten Luftstrom (100) bildet und - eine vierte Luftmenge des verdichteten Gesamtluftstroms, die geringer als die zweite Luftmenge ist, den zweiten Luftstrom (200) bildet. A method according to claim 2, characterized in that - in the first operating mode - A first amount of air of the compressed total air flow forms the first air flow (100) and - A second amount of air of the compressed total air flow forms the second air flow (200)
and in the second operating mode a third air quantity of the compressed total air flow which is equal to or less than the first air quantity, forms the first air flow (100) and - A fourth amount of air of the compressed total air flow, which is less than the second amount of air, the second air flow (200) forms. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass der dritte Luftstrom (210) in der ersten Turbine (202t) auf einen Austrittsdruck entspannt wird, der gleich dem Betriebsdruck der Hochdrucksäule (10) ist.Method according to one of claims 1 to 4, characterized in that the third air flow (210) in the first turbine (202t) is expanded to an outlet pressure which is equal to the operating pressure of the high-pressure column (10). Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass der fünfte Luftstrom (301) in der zweiten Turbine (14t) auf einen Austrittsdruck entspannt wird, der gleich dem Betriebsdruck der Hochdrucksäule (10) ist.Method according to one of claims 1 to 5, characterized in that the fifth air flow (301) in the second turbine (14t) is expanded to an outlet pressure which is equal to the operating pressure of the high-pressure column (10). Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass in dem zweiten Betriebsmodus der sechste Luftstrom (301) in der zweiten Turbine (14t) auf einen Austrittsdruck entspannt wird, der gleich dem Betriebsdruck der Niederdrucksäule (12) ist.Method according to one of claims 1 to 5, characterized in that in the second operating mode, the sixth air flow (301) in the second turbine (14t) is expanded to an outlet pressure which is equal to the operating pressure of the low pressure column (12). Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass in beiden Betriebsmodi mindestens ein Teil mindestens eines der folgenden Luftströme jeweils stromabwärts seiner Entspannung in die Hochdrucksäule (10) eingeleitet wird: - erster Luftstrom (102), - dritter Luftstrom (211), - vierter Luftstrom (234). Method according to one of claims 1 to 7, characterized in that in both modes at least a portion of at least one of the following air streams is introduced downstream of its expansion in the high-pressure column (10): first air stream (102), third airflow (211), - fourth airflow (234). Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, dass mindestens ein Teil des entspannten fünften Luftstroms (302) in die Hochdrucksäule (10) eingeleitet (13) wird.Method according to one of claims 1 to 8, characterized in that at least a portion of the expanded fifth air stream (302) in the high-pressure column (10) is introduced (13). Verfahren nach einem der Ansprüche 1 bis 13, dadurch gekennzeichnet, dass - ein zweiter Produktstrom flüssig aus dem Destillationssäulen-System abgezogen, in flüssigem Zustand auf einen zweiten erhöhten Produktdruck gebracht, in dem Hauptwärmetauscher verdampft oder pseudo-verdampft und angewärmt wird und - der angewärmte zweite Produktstrom als zweites Druckgasprodukt aus der Luftzerlegungsanlage abgezogen wird,
wobei insbesondere - der erste Produktstrom durch Sauerstoff (37) aus dem unteren Bereich der Niederdrucksäule und/oder - der zweite Produktstrom durch Stickstoff (43) aus dem oberen Bereich der Hochdrucksäule oder aus einem Kopfkondensator der Hochdrucksäule gebildet wird. Method according to one of claims 1 to 13, characterized in that a second product stream is withdrawn liquid from the distillation column system, brought to a second elevated product pressure in the liquid state, vaporized or pseudo-vaporized and heated in the main heat exchanger, and - The warmed second product stream is withdrawn as a second compressed gas product from the air separation plant,
in particular - The first product flow through oxygen (37) from the lower region of the low pressure column and / or - The second product stream is formed by nitrogen (43) from the upper region of the high pressure column or from a top condenser of the high pressure column. Luftzerlegungsanlage zur Tieftemperaturzerlegung von Luft mit - einem Hauptwärmetauscher (8), - einem Destillationssäulen-System, das eine Hochdrucksäule (10) und eine Niederdrucksäule aufweist, - einem Hauptluftverdichter (3) zum Verdichten der gesamten Einsatzluft (1) auf einen ersten Luftdruck, der mindestens 3 bar höher als der Betriebsdruck der Hochdrucksäule ist, um einen verdichteten Gesamtluftstrom (4, 7) zu bilden, - Mitteln zum Abkühlen eines ersten Teils des verdichteten Gesamtluftstroms als ersten Luftstrom (100) unter dem ersten Luftdruck in dem Hauptwärmetauscher (8), - Mitteln zum Entspannen (101) und Einleiten (102, 9) in das Destillationssäulen-System des abgekühlten ersten Luftstroms, - einem ersten turbinengetriebenen Nachverdichter (202c) zum Nachverdichten eines zweiten Teils des verdichteten Gesamtluftstroms als zweiten Luftstrom (200) auf einen zweiten Luftdruck, der höher als der erste Luftdruck ist, - einer ersten Turbine (202t) zum arbeitsleistenden Entspannen eines ersten Teilstroms des nachverdichteten zweiten Luftstroms als dritten Luftstrom (210), von dem zweiten Luftdruck und einer ersten Temperatur (T1) aus einem ersten Turbineneintrittsdruck aus, der größer als der erste Luftdruck, aber nicht größer als der dritte Luftdruck ist, wobei die erste Turbine (202t) mit dem ersten turbinengetriebenen Nachverdichter (202c) gekoppelt ist, - Mitteln zum Einleiten (211, 213, 22) des arbeitsleistend entspannten dritten Teilstroms in das Destillationssäulen-System, - Mitteln zum Gewinnen mindestens eines Flüssigprodukts (30; 39; LAR) in dem Destillationssäulen-System und Mittel zum Abziehen des Flüssigprodukts aus der Luftzerlegungsanlage, - Mitteln zum flüssigen Abziehen eines ersten Produktstroms (37; 43) aus dem Destillationssäulen-System abgezogen, zur Druckerhöhung in flüssigem Zustand auf einen ersten erhöhten Produktdruck (41; 44), zum Anwärmen in dem Hauptwärmetauscher (8) und mit - Mitteln zum Abziehen des angewärmten ersten Produktstroms (42; 45) als erstes Druckgasprodukt aus der Luftzerlegungsanlage, - Mittel zum Abkühlen eines zweiten Teilstroms des zweiten Luftstroms als vierten Luftstrom (230) in dem Hauptwärmetauscher (8) auf eine erste Zwischentemperatur T3), - einen Kaltverdichter (14c) zum Weiterverdichten des vierten Luftstroms auf einen dritten Luftdruck, der höher als der zweite Luftdruck ist, - Mittel zum Abkühlen des weiterverdichteten vierten Luftstroms unter dem dritten Luftdruck in dem Hauptwärmetauscher (8), - Mittel zum Entspannen (233) und Einleiten (234, 9) in das Destillationssäulen-System des abgekühlten vierten Luftstroms - und mit Mitteln zum Umschalten zwischen einem ersten und einem zweiten Betriebsmodus, wobei - in einem ersten Betriebsmodus eine erste Gesamtmenge an Flüssigprodukten (30; 39; LAR) aus der Luftzerlegungsanlage abgezogen wird, - in einem zweiten Betriebsmodus eine zweite Gesamtmenge an Flüssigprodukten (30; 39; LAR) aus der Luftzerlegungsanlage abgezogen wird, die geringer als die erste Gesamtmenge ist, - wobei die Mittel zum Umschalten so ausgebildet sind, dass der vierte Luftstrom (230), der durch den Kaltverdichter (14c) strömt, mindestens eine der folgenden Eigenschaften aufweist: - seine Menge ist im zweiten Betriebsmodus größer als im ersten Betriebsmodus und - sein Druck am Austritt des Kaltverdichters ist im zweiten Betriebsmodus höher als im ersten Betriebsmodus. Air separation plant for the cryogenic separation of air with a main heat exchanger (8), a distillation column system comprising a high pressure column (10) and a low pressure column, - A main air compressor (3) for compressing the total feed air (1) to a first air pressure which is at least 3 bar higher than the operating pressure of the high pressure column to form a compressed total air flow (4, 7) Means for cooling a first part of the compressed total air flow as the first air flow (100) below the first air pressure in the main heat exchanger (8), - Means for relaxing (101) and introducing (102, 9) in the distillation column system of the cooled first air stream, a first turbine-driven secondary compressor (202c) for recompressing a second part of the total compressed air flow as a second airflow (200) to a second air pressure higher than the first air pressure, - A first turbine (202t) for work-performing expansion of a first partial flow of the second secondary air flow as a third air flow (210), from the second air pressure and a first temperature (T1) from a first turbine inlet pressure, which is greater than the first air pressure, but not greater is the third air pressure, wherein the first turbine (202t) is coupled to the first turbine-driven booster (202c), - Means for introducing (211, 213, 22) of the work-performing relaxed third substream in the distillation column system, Means for recovering at least one liquid product (30; 39; LAR) in the distillation column system and means for withdrawing the liquid product from the air separation plant, - means for liquid withdrawal of a first product stream (37; 43) withdrawn from the distillation column system, for pressure increase in the liquid state to a first elevated product pressure (41; 44), for heating in the main heat exchanger (8) and with Means for drawing off the warmed first product stream (42, 45) as the first compressed gas product from the air separation plant, - means for cooling a second partial flow of the second air flow as the fourth air flow (230) in the main heat exchanger (8) to a first intermediate temperature T3), a cold compressor (14c) for further compressing the fourth air flow to a third air pressure higher than the second air pressure, Means for cooling the further compressed fourth air flow below the third air pressure in the main heat exchanger (8), - means for venting (233) and introducing (234, 9) into the distillation column system of the cooled fourth air stream - And with means for switching between a first and a second operating mode, wherein in a first mode of operation, a first total quantity of liquid products (30, 39, LAR) is withdrawn from the air separation plant, in a second operating mode, a second total quantity of liquid products (30; 39; LAR) is withdrawn from the air separation plant which is less than the first total amount, - wherein the means for switching are formed so that the fourth air flow (230) which flows through the cold compressor (14c) has at least one of the following properties: its quantity is greater in the second operating mode than in the first operating mode and - Its pressure at the outlet of the cold compressor is higher in the second operating mode than in the first operating mode.
EP15001881.0A 2014-07-05 2015-06-25 Method and device for the cryogenic decomposition of air Active EP2963369B1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PL15001881T PL2963369T3 (en) 2014-07-05 2015-06-25 Method and device for the cryogenic decomposition of air
EP15001881.0A EP2963369B1 (en) 2014-07-05 2015-06-25 Method and device for the cryogenic decomposition of air

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP14002310 2014-07-05
EP15001881.0A EP2963369B1 (en) 2014-07-05 2015-06-25 Method and device for the cryogenic decomposition of air

Publications (2)

Publication Number Publication Date
EP2963369A1 true EP2963369A1 (en) 2016-01-06
EP2963369B1 EP2963369B1 (en) 2018-05-02

Family

ID=51176037

Family Applications (1)

Application Number Title Priority Date Filing Date
EP15001881.0A Active EP2963369B1 (en) 2014-07-05 2015-06-25 Method and device for the cryogenic decomposition of air

Country Status (6)

Country Link
US (1) US11175091B2 (en)
EP (1) EP2963369B1 (en)
CN (1) CN105318661B (en)
PL (1) PL2963369T3 (en)
RU (1) RU2698378C2 (en)
TW (1) TWI663373B (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10794630B2 (en) 2017-08-03 2020-10-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating air by cryogenic distillation
EP4151940A1 (en) * 2021-09-18 2023-03-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for cryogenic air separation

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20200406183A1 (en) * 2018-03-09 2020-12-31 O2 Industries Inc. Systems, apparatus and methods for separating oxygen from air
EP3864357B1 (en) * 2018-10-09 2025-07-23 Linde GmbH Method for producing one or more air products and air separation system
CN113758150A (en) * 2021-09-18 2021-12-07 乔治洛德方法研究和开发液化空气有限公司 Method for low-temperature separation of air and air separation plant

Citations (75)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE830805C (en) 1944-11-19 1952-02-07 Linde Eismasch Ag Process for gas, especially air, separation
DE901542C (en) 1952-01-10 1954-01-11 Linde Eismasch Ag Process for the separation of air by liquefaction and rectification
US2712738A (en) 1952-01-10 1955-07-12 Linde S Eismaschinen Ag Method for fractionating air by liquefaction and rectification
DE952908C (en) 1953-10-11 1956-11-22 Linde Eismasch Ag Process for the separation of air
US2784572A (en) 1953-01-02 1957-03-12 Linde S Eismaschinen Ag Method for fractionating air by liquefaction and rectification
DE1103363B (en) 1958-09-24 1961-03-30 Linde Eismasch Ag Method and device for generating a balanced cold budget when extracting gas mixtures and / or gas mixture components under higher pressure by rectification
DE1112997B (en) 1960-08-13 1961-08-24 Linde Eismasch Ag Process and device for gas separation by rectification at low temperature
DE1117616B (en) 1960-10-14 1961-11-23 Linde Eismasch Ag Method and device for obtaining particularly pure decomposition products in cryogenic gas separation plants
DE1124529B (en) 1957-07-04 1962-03-01 Linde Eismasch Ag Method and device for carrying out heat exchange processes in a gas separation plant working with upstream regenerators
DE1187248B (en) 1963-03-29 1965-02-18 Linde Eismasch Ag Process and device for the production of oxygen gas with 70 to 98% O-content
DE1199293B (en) 1963-03-29 1965-08-26 Linde Eismasch Ag Method and device for air separation in a single column rectifier
US3216206A (en) 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances
US3222878A (en) 1962-12-21 1965-12-14 Linde Eismasch Ag Method and apparatus for fractionation of air
DE1235347B (en) 1964-05-13 1967-03-02 Linde Ag Method and device for the operation of switchable heat exchangers in low-temperature gas separation
DE1258882B (en) 1963-06-19 1968-01-18 Linde Ag Process and system for air separation by rectification using a high pressure gas refrigeration cycle for the pressure evaporation of liquid oxygen
DE1263037B (en) 1965-05-19 1968-03-14 Linde Ag Method for the separation of air in a rectification column and the separation of a gas mixture containing hydrogen
US3416323A (en) 1966-01-13 1968-12-17 Linde Ag Low temperature production of highly compressed gaseous and/or liquid oxygen
DE1501723A1 (en) 1966-01-13 1969-06-26 Linde Ag Method and device for generating gaseous high-pressure oxygen in the low-temperature rectification of air
DE2535132A1 (en) 1975-08-06 1977-02-10 Linde Ag PROCESS AND DEVICE FOR PRODUCING OXYGEN BY TWO-STAGE LOW TEMPERATURE RECTIFICATION OF AIR
DE2646690A1 (en) 1976-10-15 1978-04-20 Linde Ag Oxygen and steam mixer for cellulose bleaching - has air fractionating plant supplying liquid oxygen to steam nozzle
US4555256A (en) 1982-05-03 1985-11-26 Linde Aktiengesellschaft Process and device for the production of gaseous oxygen at elevated pressure
US5036672A (en) 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
US5263328A (en) 1991-03-26 1993-11-23 Linde Aktiengesellschaft Process for low-temperature air fractionation
US5644934A (en) 1994-12-05 1997-07-08 Linde Aktiengesellchaft Process and device for low-temperature separation of air
US5845517A (en) 1995-08-11 1998-12-08 Linde Aktiengesellschaft Process and device for air separation by low-temperature rectification
DE19803437A1 (en) 1998-01-29 1999-03-18 Linde Ag Oxygen and nitrogen extracted by low-temperature fractional distillation
US5953937A (en) 1995-07-21 1999-09-21 Linde Aktiengesellschaft Process and apparatus for the variable production of a gaseous pressurized product
EP0955509A1 (en) 1998-04-30 1999-11-10 Linde Aktiengesellschaft Process and apparatus to produce high purity nitrogen
US6038885A (en) 1997-07-30 2000-03-21 Linde Aktiengesellschaft Air separation process
DE19909744A1 (en) 1999-03-05 2000-05-04 Linde Ag Low-temperature air fractionating system re-compresses nitrogen-containing fraction separate from input air using indirect exchange for fraction heating.
EP1031804A1 (en) 1999-02-26 2000-08-30 Linde Technische Gase GmbH Air separation process with nitrogen recycling
DE19954593A1 (en) 1999-11-12 2000-09-28 Linde Ag Fractionated distillation of air to oxygen and nitrogen uses little energy and facilitates the production of oxygen of any purity level
DE10013073A1 (en) 2000-03-17 2000-10-19 Linde Ag Low temperature separation of air in distillation column system uses integrated heat exchanger system for cooling e.g. air supply by indirect heat exchange during vaporization of first liquid fraction
EP1067345A1 (en) 1999-07-05 2001-01-10 Linde Aktiengesellschaft Process and device for cryogenic air separation
EP1074805A1 (en) 1999-08-05 2001-02-07 Linde Aktiengesellschaft Process for producing oxygen under pressure and device therefor
US6185960B1 (en) 1998-04-08 2001-02-13 Linde Aktiengesellschaft Process and device for the production of a pressurized gaseous product by low-temperature separation of air
EP1134525A1 (en) 2000-03-17 2001-09-19 Linde Aktiengesellschaft Process for producing gaseous and liquid nitrogen with a variable quantity of liquid
EP1139046A1 (en) 2000-03-29 2001-10-04 Linde Aktiengesellschaft Process and device for producing a high pressure product by cryogenic air separation
EP1146301A1 (en) 2000-04-12 2001-10-17 Linde Gas Aktiengesellschaft Process and apparatus for the production of high pressure nitrogen from air separation
EP1150082A1 (en) 2000-04-28 2001-10-31 Linde Aktiengesellschaft Method and apparatus for heat exchange
US6314755B1 (en) 1999-02-26 2001-11-13 Linde Aktiengesellschaft Double column system for the low-temperature fractionation of air
EP1213552A1 (en) 2000-12-06 2002-06-12 Linde Aktiengesellschaft Engine system for the work expansion of two process streams
DE10115258A1 (en) 2001-03-28 2002-07-18 Linde Ag Machine system comprises relaxation machine for reducing pressure of first process fluid mechanically coupled to pump for increasing pressure of second process fluid present in liquid form
DE10213212A1 (en) 2002-03-25 2002-10-17 Linde Ag Air fractionation plant in which product stream is split, carries out all compression stages in common dual flow pump
DE10213211A1 (en) 2002-03-25 2002-10-17 Linde Ag Air fractionation in columns producing liquid and gaseous products, exchanges heat with circuit containing recirculated cryogenic liquid
EP1284404A1 (en) 2001-08-13 2003-02-19 Linde Aktiengesellschaft Process and device for recovering a product under pressure by cryogenic air separation
EP1308680A1 (en) 2001-10-31 2003-05-07 Linde AG Process and system for production of krypton and/or xenon by cryogenic air separation
DE10238282A1 (en) 2002-08-21 2003-05-28 Linde Ag Process for the low temperature decomposition of air comprises feeding a first process air stream into a high pressure column, producing a first oxygen-enriched fraction in the high pressure column, and further processing
DE10302389A1 (en) 2003-01-22 2003-06-18 Linde Ag Device for the low temperature decomposition of air comprises a rectification system consisting of a high pressure column, a low pressure column, and a condenser-evaporator system for heating the low pressure column
EP1357342A1 (en) 2002-04-17 2003-10-29 Linde Aktiengesellschaft Cryogenic triple column air separation system with argon recovery
DE10332863A1 (en) 2003-07-18 2004-02-26 Linde Ag Krypton and xenon recovery by low-temperature fractionation of air yields higher purity products and higher argon productivity, using low nitrogen content scrubbing liquid stream
DE10334559A1 (en) 2003-05-28 2004-12-16 Linde Ag Process for recovering krypton/xenon by the cryogenic separation of air comprises feeding an argon-enriched vapor from a crude argon rectification system into a sump evaporator
DE10334560A1 (en) 2003-05-28 2004-12-16 Linde Ag Method for recovering krypton and xenon from air, comprises separating nitrogen and oxygen and feeding krypton- and xenon-containing fraction into enrichment column, stream of pure air being decompressed and fed into column
US20050126221A1 (en) * 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation
EP1544559A1 (en) 2003-12-20 2005-06-22 Linde AG Process and device for the cryogenic separation of air
EP1585926A1 (en) 2002-12-19 2005-10-19 Karges-Faulconbridge, Inc. System for liquid extraction, and methods
DE102005029274A1 (en) 2004-08-17 2006-02-23 Linde Ag Obtaining gaseous pressure product, by cryogenic separation of air implementing normal operation, emergency operation, and bypass operation
EP1666824A1 (en) 2004-12-03 2006-06-07 Linde Aktiengesellschaft Process and device for the recovery of Argon by cryogenic separation of air
EP1672301A1 (en) 2004-12-03 2006-06-21 Linde AG Apparatus for the cryogenic separation of a gaseous mixture in particular of air
DE102005028012A1 (en) 2005-06-16 2006-09-14 Linde Ag Separation of air into nitrogen and oxygen at low temperatures, with a distillation column system, uses liquefied natural gas
DE102006032731A1 (en) 2006-07-14 2007-01-18 Linde Ag Air separation process for producing nitrogen-enriched and oxygen-enriched streams comprises introducing an instrument air stream into a gas pressure reservoir
WO2007033838A1 (en) 2005-09-23 2007-03-29 Linde Aktiengesellschaft Air cryogenic separation method and device
WO2007104449A1 (en) 2006-03-15 2007-09-20 Linde Aktiengesellschaft Method and apparatus for fractionating air at low temperatures
DE102007014643A1 (en) 2007-03-27 2007-09-20 Linde Ag Method for producing gaseous pressurized product by low temperature separation of air entails first and fourth partial air flows being expanded in turbines, and second and third partial flows compressed in post-compressors
EP1845324A1 (en) 2006-04-13 2007-10-17 Linde Aktiengesellschaft Process and device for producing a high pressure product by cryogenic air separation
EP1892490A1 (en) 2006-08-16 2008-02-27 Linde Aktiengesellschaft Method and device for the production of variable amounts of a pressurized product by cryogenic gas separation
EP2015012A2 (en) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Process for the cryogenic separation of air
EP2015013A2 (en) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Process and device for producing a gaseous pressurised product by cryogenic separation of air
EP2026024A1 (en) 2007-07-30 2009-02-18 Linde Aktiengesellschaft Process and device for producing argon by cryogenic separation of air
US20090078001A1 (en) 2003-05-05 2009-03-26 L'air Liquide Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et Cryogenic Distillation Method and System for Air Separation
WO2009095188A2 (en) 2008-01-28 2009-08-06 Linde Aktiengesellschaft Method and device for low-temperature air separation
DE102008016355A1 (en) 2008-03-29 2009-10-01 Linde Ag Air cryogenic separation method for electrical energy at integrated gasification combined cycle power plant, involves bringing nitrogen flow into indirect exchange with partial flow in condenser-evaporator
EP2447563A2 (en) 2010-10-29 2012-05-02 KNORR-BREMSE Systeme für Nutzfahrzeuge GmbH Disc brake with a self-reinforcement device
EP2458311A1 (en) * 2010-11-25 2012-05-30 Linde Aktiengesellschaft Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air
EP2520886A1 (en) * 2011-05-05 2012-11-07 Linde AG Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU787829A1 (en) * 1976-09-10 1980-12-15 Предприятие П/Я А-3605 Method of producing liquid and gaseous components of air
US7272954B2 (en) * 2004-07-14 2007-09-25 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Proceded Georges Claude Low temperature air separation process for producing pressurized gaseous product
DE102010052544A1 (en) * 2010-11-25 2012-05-31 Linde Ag Process for obtaining a gaseous product by cryogenic separation of air
CN102564064A (en) * 2010-11-25 2012-07-11 林德股份公司 Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air
FR2973487B1 (en) * 2011-03-31 2018-01-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude PROCESS AND APPARATUS FOR PRODUCING PRESSURIZED AIR GAS BY CRYOGENIC DISTILLATION

Patent Citations (100)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE830805C (en) 1944-11-19 1952-02-07 Linde Eismasch Ag Process for gas, especially air, separation
DE901542C (en) 1952-01-10 1954-01-11 Linde Eismasch Ag Process for the separation of air by liquefaction and rectification
US2712738A (en) 1952-01-10 1955-07-12 Linde S Eismaschinen Ag Method for fractionating air by liquefaction and rectification
US2784572A (en) 1953-01-02 1957-03-12 Linde S Eismaschinen Ag Method for fractionating air by liquefaction and rectification
DE952908C (en) 1953-10-11 1956-11-22 Linde Eismasch Ag Process for the separation of air
DE1124529B (en) 1957-07-04 1962-03-01 Linde Eismasch Ag Method and device for carrying out heat exchange processes in a gas separation plant working with upstream regenerators
US3083544A (en) 1958-09-24 1963-04-02 Linde S Eismaschinen Ag Hollri Rectification of gases
DE1103363B (en) 1958-09-24 1961-03-30 Linde Eismasch Ag Method and device for generating a balanced cold budget when extracting gas mixtures and / or gas mixture components under higher pressure by rectification
US3214925A (en) 1960-08-13 1965-11-02 Linde Eismasch Ag System for gas separation by rectification at low temperatures
DE1112997B (en) 1960-08-13 1961-08-24 Linde Eismasch Ag Process and device for gas separation by rectification at low temperature
US3280574A (en) 1960-10-14 1966-10-25 Linde Ag High pressure pure gas for preventing contamination by low pressure raw gas in reversing regenerators
DE1117616B (en) 1960-10-14 1961-11-23 Linde Eismasch Ag Method and device for obtaining particularly pure decomposition products in cryogenic gas separation plants
US3216206A (en) 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances
DE1226616B (en) 1961-11-29 1966-10-13 Linde Ag Process and device for the production of gaseous pressurized oxygen with simultaneous production of liquid decomposition products by low-temperature air separation
US3222878A (en) 1962-12-21 1965-12-14 Linde Eismasch Ag Method and apparatus for fractionation of air
DE1229561B (en) 1962-12-21 1966-12-01 Linde Ag Method and device for separating air by liquefaction and rectification with the aid of an inert gas cycle
US3371496A (en) 1963-03-29 1968-03-05 Linde Ag Wash liquid production by heat exchange with low pressure liquid oxygen
DE1187248B (en) 1963-03-29 1965-02-18 Linde Eismasch Ag Process and device for the production of oxygen gas with 70 to 98% O-content
DE1199293B (en) 1963-03-29 1965-08-26 Linde Eismasch Ag Method and device for air separation in a single column rectifier
US3426543A (en) 1963-06-19 1969-02-11 Linde Ag Combining pure liquid and vapor nitrogen streams from air separation for crude hydrogen gas washing
DE1258882B (en) 1963-06-19 1968-01-18 Linde Ag Process and system for air separation by rectification using a high pressure gas refrigeration cycle for the pressure evaporation of liquid oxygen
DE1235347B (en) 1964-05-13 1967-03-02 Linde Ag Method and device for the operation of switchable heat exchangers in low-temperature gas separation
DE1263037B (en) 1965-05-19 1968-03-14 Linde Ag Method for the separation of air in a rectification column and the separation of a gas mixture containing hydrogen
US3401531A (en) 1965-05-19 1968-09-17 Linde Ag Heat exchange of compressed nitrogen and liquid oxygen in ammonia synthesis feed gas production
DE1501723A1 (en) 1966-01-13 1969-06-26 Linde Ag Method and device for generating gaseous high-pressure oxygen in the low-temperature rectification of air
DE1501722A1 (en) 1966-01-13 1969-06-26 Linde Ag Process for cryogenic air separation for the production of highly compressed gaseous and / or liquid oxygen
US3416323A (en) 1966-01-13 1968-12-17 Linde Ag Low temperature production of highly compressed gaseous and/or liquid oxygen
US3500651A (en) 1966-01-13 1970-03-17 Linde Ag Production of high pressure gaseous oxygen by low temperature rectification of air
DE2535132A1 (en) 1975-08-06 1977-02-10 Linde Ag PROCESS AND DEVICE FOR PRODUCING OXYGEN BY TWO-STAGE LOW TEMPERATURE RECTIFICATION OF AIR
US4279631A (en) 1975-08-06 1981-07-21 Linde Aktiengesellschaft Process and apparatus for the production of oxygen by two-stage low-temperature rectification of air
DE2646690A1 (en) 1976-10-15 1978-04-20 Linde Ag Oxygen and steam mixer for cellulose bleaching - has air fractionating plant supplying liquid oxygen to steam nozzle
US4555256A (en) 1982-05-03 1985-11-26 Linde Aktiengesellschaft Process and device for the production of gaseous oxygen at elevated pressure
EP0093448B1 (en) 1982-05-03 1986-10-15 Linde Aktiengesellschaft Process and apparatus for obtaining gaseous oxygen at elevated pressure
EP0384483B1 (en) 1989-02-23 1992-07-22 Linde Aktiengesellschaft Air rectification process and apparatus
US5036672A (en) 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
US5263328A (en) 1991-03-26 1993-11-23 Linde Aktiengesellschaft Process for low-temperature air fractionation
EP0505812B1 (en) 1991-03-26 1995-10-18 Linde Aktiengesellschaft Low temperature air separation process
US5644934A (en) 1994-12-05 1997-07-08 Linde Aktiengesellchaft Process and device for low-temperature separation of air
EP0716280B1 (en) 1994-12-05 2001-05-16 Linde Aktiengesellschaft Method and apparatus for the low temperature air separation
US5953937A (en) 1995-07-21 1999-09-21 Linde Aktiengesellschaft Process and apparatus for the variable production of a gaseous pressurized product
EP0842385B1 (en) 1995-07-21 2001-04-18 Linde Aktiengesellschaft Method and device for the production of variable amounts of a pressurized gaseous product
US5845517A (en) 1995-08-11 1998-12-08 Linde Aktiengesellschaft Process and device for air separation by low-temperature rectification
EP0758733B1 (en) 1995-08-11 2000-11-02 Linde Aktiengesellschaft Air separation process and apparatus by low temperature rectification
US6038885A (en) 1997-07-30 2000-03-21 Linde Aktiengesellschaft Air separation process
EP0895045B1 (en) 1997-07-30 2002-11-27 Linde Aktiengesellschaft Air separation process
DE19803437A1 (en) 1998-01-29 1999-03-18 Linde Ag Oxygen and nitrogen extracted by low-temperature fractional distillation
EP0949471B1 (en) 1998-04-08 2002-12-18 Linde AG Cryogenic air separation plant with two different operation modes
US6185960B1 (en) 1998-04-08 2001-02-13 Linde Aktiengesellschaft Process and device for the production of a pressurized gaseous product by low-temperature separation of air
US6196022B1 (en) 1998-04-30 2001-03-06 Linde Aktiengesellschaft Process and device for recovering high-purity oxygen
EP0955509A1 (en) 1998-04-30 1999-11-10 Linde Aktiengesellschaft Process and apparatus to produce high purity nitrogen
US6314755B1 (en) 1999-02-26 2001-11-13 Linde Aktiengesellschaft Double column system for the low-temperature fractionation of air
EP1031804A1 (en) 1999-02-26 2000-08-30 Linde Technische Gase GmbH Air separation process with nitrogen recycling
DE19909744A1 (en) 1999-03-05 2000-05-04 Linde Ag Low-temperature air fractionating system re-compresses nitrogen-containing fraction separate from input air using indirect exchange for fraction heating.
EP1067345A1 (en) 1999-07-05 2001-01-10 Linde Aktiengesellschaft Process and device for cryogenic air separation
US6336345B1 (en) 1999-07-05 2002-01-08 Linde Aktiengesellschaft Process and apparatus for low temperature fractionation of air
EP1074805A1 (en) 1999-08-05 2001-02-07 Linde Aktiengesellschaft Process for producing oxygen under pressure and device therefor
US6332337B1 (en) 1999-08-05 2001-12-25 Linde Aktiengesellschaft Method and apparatus for recovering oxygen at hyperbaric pressure
DE19954593A1 (en) 1999-11-12 2000-09-28 Linde Ag Fractionated distillation of air to oxygen and nitrogen uses little energy and facilitates the production of oxygen of any purity level
EP1134525A1 (en) 2000-03-17 2001-09-19 Linde Aktiengesellschaft Process for producing gaseous and liquid nitrogen with a variable quantity of liquid
US6477860B2 (en) 2000-03-17 2002-11-12 Linde Aktiengesellschaft Process for obtaining gaseous and liquid nitrogen with a variable proportion of liquid product
DE10013073A1 (en) 2000-03-17 2000-10-19 Linde Ag Low temperature separation of air in distillation column system uses integrated heat exchanger system for cooling e.g. air supply by indirect heat exchange during vaporization of first liquid fraction
EP1139046A1 (en) 2000-03-29 2001-10-04 Linde Aktiengesellschaft Process and device for producing a high pressure product by cryogenic air separation
EP1146301A1 (en) 2000-04-12 2001-10-17 Linde Gas Aktiengesellschaft Process and apparatus for the production of high pressure nitrogen from air separation
EP1150082A1 (en) 2000-04-28 2001-10-31 Linde Aktiengesellschaft Method and apparatus for heat exchange
EP1213552A1 (en) 2000-12-06 2002-06-12 Linde Aktiengesellschaft Engine system for the work expansion of two process streams
DE10115258A1 (en) 2001-03-28 2002-07-18 Linde Ag Machine system comprises relaxation machine for reducing pressure of first process fluid mechanically coupled to pump for increasing pressure of second process fluid present in liquid form
EP1284404A1 (en) 2001-08-13 2003-02-19 Linde Aktiengesellschaft Process and device for recovering a product under pressure by cryogenic air separation
US20030051504A1 (en) 2001-08-13 2003-03-20 Linde Aktiengesellschaft Process and device for obtaining a compressed product by low temperature separation of air
US6612129B2 (en) 2001-10-31 2003-09-02 Linde Aktiengesellschaft Process and apparatus for producing krypton and/or xenon by low-temperature fractionation of air
EP1308680A1 (en) 2001-10-31 2003-05-07 Linde AG Process and system for production of krypton and/or xenon by cryogenic air separation
DE10213211A1 (en) 2002-03-25 2002-10-17 Linde Ag Air fractionation in columns producing liquid and gaseous products, exchanges heat with circuit containing recirculated cryogenic liquid
DE10213212A1 (en) 2002-03-25 2002-10-17 Linde Ag Air fractionation plant in which product stream is split, carries out all compression stages in common dual flow pump
EP1357342A1 (en) 2002-04-17 2003-10-29 Linde Aktiengesellschaft Cryogenic triple column air separation system with argon recovery
DE10238282A1 (en) 2002-08-21 2003-05-28 Linde Ag Process for the low temperature decomposition of air comprises feeding a first process air stream into a high pressure column, producing a first oxygen-enriched fraction in the high pressure column, and further processing
EP1585926A1 (en) 2002-12-19 2005-10-19 Karges-Faulconbridge, Inc. System for liquid extraction, and methods
DE10302389A1 (en) 2003-01-22 2003-06-18 Linde Ag Device for the low temperature decomposition of air comprises a rectification system consisting of a high pressure column, a low pressure column, and a condenser-evaporator system for heating the low pressure column
US20090078001A1 (en) 2003-05-05 2009-03-26 L'air Liquide Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et Cryogenic Distillation Method and System for Air Separation
DE10334560A1 (en) 2003-05-28 2004-12-16 Linde Ag Method for recovering krypton and xenon from air, comprises separating nitrogen and oxygen and feeding krypton- and xenon-containing fraction into enrichment column, stream of pure air being decompressed and fed into column
DE10334559A1 (en) 2003-05-28 2004-12-16 Linde Ag Process for recovering krypton/xenon by the cryogenic separation of air comprises feeding an argon-enriched vapor from a crude argon rectification system into a sump evaporator
DE10332863A1 (en) 2003-07-18 2004-02-26 Linde Ag Krypton and xenon recovery by low-temperature fractionation of air yields higher purity products and higher argon productivity, using low nitrogen content scrubbing liquid stream
US20050126221A1 (en) * 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation
EP1544559A1 (en) 2003-12-20 2005-06-22 Linde AG Process and device for the cryogenic separation of air
DE102005029274A1 (en) 2004-08-17 2006-02-23 Linde Ag Obtaining gaseous pressure product, by cryogenic separation of air implementing normal operation, emergency operation, and bypass operation
EP1666824A1 (en) 2004-12-03 2006-06-07 Linde Aktiengesellschaft Process and device for the recovery of Argon by cryogenic separation of air
EP1672301A1 (en) 2004-12-03 2006-06-21 Linde AG Apparatus for the cryogenic separation of a gaseous mixture in particular of air
DE102005028012A1 (en) 2005-06-16 2006-09-14 Linde Ag Separation of air into nitrogen and oxygen at low temperatures, with a distillation column system, uses liquefied natural gas
WO2007033838A1 (en) 2005-09-23 2007-03-29 Linde Aktiengesellschaft Air cryogenic separation method and device
WO2007104449A1 (en) 2006-03-15 2007-09-20 Linde Aktiengesellschaft Method and apparatus for fractionating air at low temperatures
EP1845324A1 (en) 2006-04-13 2007-10-17 Linde Aktiengesellschaft Process and device for producing a high pressure product by cryogenic air separation
DE102006032731A1 (en) 2006-07-14 2007-01-18 Linde Ag Air separation process for producing nitrogen-enriched and oxygen-enriched streams comprises introducing an instrument air stream into a gas pressure reservoir
EP1892490A1 (en) 2006-08-16 2008-02-27 Linde Aktiengesellschaft Method and device for the production of variable amounts of a pressurized product by cryogenic gas separation
DE102007014643A1 (en) 2007-03-27 2007-09-20 Linde Ag Method for producing gaseous pressurized product by low temperature separation of air entails first and fourth partial air flows being expanded in turbines, and second and third partial flows compressed in post-compressors
EP2015012A2 (en) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Process for the cryogenic separation of air
EP2015013A2 (en) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Process and device for producing a gaseous pressurised product by cryogenic separation of air
EP2026024A1 (en) 2007-07-30 2009-02-18 Linde Aktiengesellschaft Process and device for producing argon by cryogenic separation of air
WO2009095188A2 (en) 2008-01-28 2009-08-06 Linde Aktiengesellschaft Method and device for low-temperature air separation
DE102008016355A1 (en) 2008-03-29 2009-10-01 Linde Ag Air cryogenic separation method for electrical energy at integrated gasification combined cycle power plant, involves bringing nitrogen flow into indirect exchange with partial flow in condenser-evaporator
EP2447563A2 (en) 2010-10-29 2012-05-02 KNORR-BREMSE Systeme für Nutzfahrzeuge GmbH Disc brake with a self-reinforcement device
EP2458311A1 (en) * 2010-11-25 2012-05-30 Linde Aktiengesellschaft Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air
EP2520886A1 (en) * 2011-05-05 2012-11-07 Linde AG Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
HAUSEN; LINDE: "Tieftemperaturtechnik 2. Auflage", 1985, article "Kapitel 4", pages: 281 - 337

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10794630B2 (en) 2017-08-03 2020-10-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating air by cryogenic distillation
US10866024B2 (en) 2017-08-03 2020-12-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device and method for separating air by cryogenic distillation
US12181217B2 (en) 2017-08-03 2024-12-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus and method for separation of air by cryogenic distillation
EP4151940A1 (en) * 2021-09-18 2023-03-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for cryogenic air separation

Also Published As

Publication number Publication date
RU2015126802A (en) 2017-01-13
US20160003535A1 (en) 2016-01-07
TWI663373B (en) 2019-06-21
CN105318661A (en) 2016-02-10
US11175091B2 (en) 2021-11-16
RU2698378C2 (en) 2019-08-26
TW201629415A (en) 2016-08-16
CN105318661B (en) 2019-08-06
PL2963369T3 (en) 2018-10-31
EP2963369B1 (en) 2018-05-02
RU2015126802A3 (en) 2019-02-08

Similar Documents

Publication Publication Date Title
EP3164654B1 (en) Method and device for the low-temperature separation of air at variable energy consumption
EP2963370B1 (en) Method and device for the cryogenic decomposition of air
EP1067345B1 (en) Process and device for cryogenic air separation
EP1994344A1 (en) Method and apparatus for fractionating air at low temperatures
DE102010052545A1 (en) Method and apparatus for recovering a gaseous product by cryogenic separation of air
EP3410050B1 (en) Method for producing one or more air products and air separation system
EP1139046A1 (en) Process and device for producing a high pressure product by cryogenic air separation
EP3179187B1 (en) Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus
EP2466236A1 (en) Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air
EP2015012A2 (en) Process for the cryogenic separation of air
EP3290843A2 (en) Method and device for extracting pressurised nitrogen and pressurised nitrogen by cryogenic decomposition of air
EP2299221A2 (en) Method and device for cryogenic decomposition of air
EP2963369B1 (en) Method and device for the cryogenic decomposition of air
EP2520886A1 (en) Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air
EP2053331A1 (en) Method and device for low-temperature air separation
WO2020164799A1 (en) Method and system for providing one or more oxygen-rich, gaseous air products
WO2014154361A2 (en) Method and device for producing gaseous compressed oxygen having variable power consumption
EP2551619A1 (en) Method and device for extracting pressurised oxygen and pressurised nitrogen by cryogenic decomposition of air
DE102007042462A1 (en) Method and apparatus for the cryogenic separation of air
WO2011110301A2 (en) Method and device for cryogenic separation of air
EP2600090A1 (en) Method and device for generating pressurised oxygen by cryogenic decomposition of air
WO2014037091A2 (en) Process and facility for generating liquid and gaseous oxygen products by low-temperature separation of air
EP2963371B1 (en) Method and device for creating a pressurised gas product by the cryogenic decomposition of air
DE102010055448A1 (en) Method and apparatus for the cryogenic separation of air
EP4495524A1 (en) Process and device for the low-temperature separation of air, comprising the recovery of a krypton-xenon concentrate

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

17P Request for examination filed

Effective date: 20160630

RBV Designated contracting states (corrected)

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20171218

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 4

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

Ref country code: AT

Ref legal event code: REF

Ref document number: 995718

Country of ref document: AT

Kind code of ref document: T

Effective date: 20180515

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 502015004064

Country of ref document: DE

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: GERMAN

REG Reference to a national code

Ref country code: NL

Ref legal event code: FP

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180802

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180802

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180803

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 502015004064

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180625

26N No opposition filed

Effective date: 20190205

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180625

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180630

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180630

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MK

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180502

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20150625

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180502

REG Reference to a national code

Ref country code: DE

Ref legal event code: R081

Ref document number: 502015004064

Country of ref document: DE

Owner name: LINDE GMBH, DE

Free format text: FORMER OWNER: LINDE AKTIENGESELLSCHAFT, 80331 MUENCHEN, DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180902

REG Reference to a national code

Ref country code: AT

Ref legal event code: MM01

Ref document number: 995718

Country of ref document: AT

Kind code of ref document: T

Effective date: 20200625

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200625

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20250618

Year of fee payment: 11

Ref country code: PL

Payment date: 20250613

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20250620

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20250618

Year of fee payment: 11

Ref country code: BE

Payment date: 20250617

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20250626

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20250630

Year of fee payment: 11