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US20110197630A1 - Process and Apparatus for the Separation of Air by Cryogenic Distillation - Google Patents

Process and Apparatus for the Separation of Air by Cryogenic Distillation Download PDF

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Publication number
US20110197630A1
US20110197630A1 US12/671,927 US67192711A US2011197630A1 US 20110197630 A1 US20110197630 A1 US 20110197630A1 US 67192711 A US67192711 A US 67192711A US 2011197630 A1 US2011197630 A1 US 2011197630A1
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United States
Prior art keywords
air
compressor
heat exchange
mode
sending
Prior art date
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Abandoned
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US12/671,927
Inventor
Alain Guillard
Lasad Jaouani
Xavier Pontone
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.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Assigned to L'AIR LIQUIDE SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GUILLARD, ALAIN, JAOUANI, LASAD, PONTONE, XAVIER
Publication of US20110197630A1 publication Critical patent/US20110197630A1/en
Abandoned legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • F25J3/04006—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
    • F25J3/0409—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
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • 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
    • 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
    • F25J3/04763—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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • 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
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air

Definitions

  • the present invention relates to a process and apparatus for the separation of air by cryogenic distillation.
  • the present invention allows the apparatus to function with optimal power consumption during both modes of operation.
  • the apparatus includes an air separation column system which may be of any known type, but may particularly be a double column system including a high pressure column and a low pressure column, thermally coupled via a reboiler condenser at the bottom of the low pressure column wherein nitrogen from the top of the high pressure column is condensed.
  • an air separation column system which may be of any known type, but may particularly be a double column system including a high pressure column and a low pressure column, thermally coupled via a reboiler condenser at the bottom of the low pressure column wherein nitrogen from the top of the high pressure column is condensed.
  • a process for the production of at least one liquid product and at least one gaseous product by cryogenic distillation of air under a first mode of operation and a second mode of operation the process producing more liquid as final product during the second mode than during the first mode
  • compressed and purified gaseous air is cooled in a heat exchange line and sent to at least one column of a column system
  • a liquid stream enriched in a component of air is removed from a column of the column system and vaporised in the heat exchange line
  • air at an elevated pressure is sent to the heat exchange line
  • condensed and sent to the column system and part of the feed air is sent to one of at least two expanders and thence to a column of the column system
  • all of the feed air is compressed to a high pressure at least 20 bars higher than the highest column pressure of the column system in a second compressor, cooled in the heat exchange line and sent in part to a column system, another part of the high pressure air being sent to the second expander.
  • an apparatus for the separation of air by cryogenic distillation comprising:
  • FIGS. 1 , 2 and 3 show air flow diagrams for an air separation unit according to the invention.
  • the dashed lines indicate couplings between a compressor and a turbine.
  • FIG. 1 uses a double column system in which a high pressure column 65 is placed underneath a low pressure column 67 and thermally coupled thereto via a reboiler condenser 69 .
  • cooled, purified and compressed gaseous air is fed to the high pressure column 65 .
  • Reflux streams (not shown) are sent from the high pressure column to the low pressure column 67 as is well known in the art.
  • gaseous nitrogen 61 is removed from the top of the low pressure column 67 and warmed in exchanger 19 whilst waste nitrogen 59 is removed from lower down the low pressure column 67 and warmed in exchanger 19 before being used to regenerate the purification unit 8 .
  • FIG. 1 all the air is compressed to 15.5 bars in compressor 1 and cooled in cooler 4 to form stream 3 . Following further cooling in cooler 6 , the air is purified in purification unit 8 .
  • the outlet of compressor 1 is connected to the inlet of compressor 5 and to the heat exchanger 19 .
  • liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • liquid oxygen LOX 53 and liquid nitrogen LIN 69 are removed from the low pressure and high pressure columns respectively.
  • liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • the cooling section 43 receives air at 47 bars which is then cooled by passing through the whole heat exchange line during the liquid mode and receives air at 26 bars coming from the cold compressor 37 during the gas mode.
  • section 28 sees a reversal of flow between the two modes, air flowing in one direction from the heat exchange line 19 to the turbine 29 in liquid mode and in the other direction from the cold compressor 37 to the heat exchange line 19 in gas mode.
  • the nitrogen 61 is compressed to a higher pressure in compressor 63 .
  • liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • liquid oxygen LOX 53 and liquid nitrogen LIN 69 are removed from the low pressure and high pressure columns respectively.
  • liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • the cooling section 43 receives air which is then cooled by passing through the whole heat exchange line during the liquid mode and receives air at 26 bars coming from the cold compressor 37 during the gas mode.
  • section 23 sees a reversal of flow between the two modes, air flowing in one direction from the heat exchange line 19 to the turbine 29 in liquid mode and in the other direction from the cold compressor 37 to the heat exchange line 19 in gas mode.
  • the nitrogen 61 is compressed to a higher pressure in compressor 63 .
  • FIG. 3 In a simplified version of FIG. 1 , as shown in FIG. 3 , only two air turbines are used.
  • FIG. 3 may use a double column system as shown and described for FIG. 1 , in which a high pressure column 65 is placed underneath a low pressure column 67 and thermally coupled thereto via a reboiler condenser 69 .
  • cooled, purified and compressed gaseous air is fed to the high pressure column 65 .
  • Reflux streams (not shown) are sent from the high pressure column to the low pressure column 67 as is well known in the art.
  • gaseous nitrogen 61 is removed from the top of the low pressure column 67 and warmed in exchanger 19 whilst waste nitrogen 59 is removed from lower down the low pressure column 67 and warmed in exchanger 19 before being used to regenerate the purification unit 8 .
  • liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • the cooling section 43 receives air at 47 bars which is then cooled by passing through the whole heat exchange line during the liquid mode and receives air at 26 bars coming from the cold compressor 37 during the gas mode.
  • section 23 sees a reversal of flow between the two modes, air flowing in one direction from the heat exchange line 19 to the turbine 29 in liquid mode and in the other direction from the cold compressor 37 to the heat exchange line 19 in gas mode.

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

Abstract

A process and apparatus for the separation of air by cryogenic distillation is provided.

Description

  • The present invention relates to a process and apparatus for the separation of air by cryogenic distillation.
  • It is frequently desirable to have an air separation unit which produces at least mainly gas during at least one period when electricity costs are higher and at least mainly liquid during at least one period when electricity costs are lower. The present invention allows the apparatus to function with optimal power consumption during both modes of operation.
  • The apparatus includes an air separation column system which may be of any known type, but may particularly be a double column system including a high pressure column and a low pressure column, thermally coupled via a reboiler condenser at the bottom of the low pressure column wherein nitrogen from the top of the high pressure column is condensed.
  • All pressures mentioned in this text are absolute pressures.
  • According to an object of the invention, there is provided a process for the production of at least one liquid product and at least one gaseous product by cryogenic distillation of air under a first mode of operation and a second mode of operation, the process producing more liquid as final product during the second mode than during the first mode wherein in all modes of operation, compressed and purified gaseous air is cooled in a heat exchange line and sent to at least one column of a column system, a liquid stream enriched in a component of air is removed from a column of the column system and vaporised in the heat exchange line, air at an elevated pressure is sent to the heat exchange line, condensed and sent to the column system and part of the feed air is sent to one of at least two expanders and thence to a column of the column system wherein
  • i) according to the first mode, at least part of the feed air is removed from an intermediate point of the heat exchange line, compressed at a cryogenic temperature in a cold compressor and sent to the heat exchange line to be further cooled and sent to the column system and part of the feed air is sent to the first expander and
  • ii) according to the second mode, all of the feed air is compressed to a high pressure at least 20 bars higher than the highest column pressure of the column system in a second compressor, cooled in the heat exchange line and sent in part to a column system, another part of the high pressure air being sent to the second expander.
  • According to optional aspects of the invention:
      • according to the first mode, part of the feed air at the outlet pressure of the cold compressor is cooled and sent to the first expander;
      • the cold compressor is coupled to the first expander;
      • the second compressor is coupled to the second expander;
      • air treated in the second compressor in the second mode and in the cold compressor in the first mode is subsequently sent to a common transfer means upstream of the column system;
      • in the first mode the air is sent from the cold compressor to the heat exchange line via a conduit and in the second mode the air is sent from the second compressor to the second expander via the same conduit;
      • in the first mode the air is sent from the cold compressor via a passage of the heat exchange line to the cold end thereof and in the second mode the air is sent from the second compressor to the cold end of the heat exchange line via the same passage.
  • According to a further aspect of the invention, there is provided an apparatus for the separation of air by cryogenic distillation comprising:
  • a) a column system
  • b) a heat exchange line
  • c) a main compressor
  • d) a cold compressor connected to the outlet of the main compressor
  • e) a second compressor connected to the outlet of the main compressor
  • f) first and second expanders
  • g) means for sending air from the cold compressor to the first expander
  • h) means for sending air from the second compressor to the second expander
  • i) means for sending air from the first and second expanders to the column system
  • j) means for sending air from the cold compressor and the second compressor to the column system via the heat exchange means without traversing either of the first and second expanders.
  • According to further optional aspects:
      • the means for sending air from the cold compressor to the first expander and means for sending air from the second compressor to the second expander include a common section of conduit;
      • the means for sending air from the cold compressor and the second compressor to the column system via the heat exchange means without traversing either of the first and second expanders includes at least one common passage in the heat exchange means;
      • the apparatus includes a third expander and means for sending air from the column system to the third expander and thence to the heat exchange means.
  • The invention will be described in more detail with reference to the Figures. FIGS. 1, 2 and 3 show air flow diagrams for an air separation unit according to the invention. The dashed lines indicate couplings between a compressor and a turbine.
    •
  • The process of FIG. 1 uses a double column system in which a high pressure column 65 is placed underneath a low pressure column 67 and thermally coupled thereto via a reboiler condenser 69.
  • In all the modes of operation, cooled, purified and compressed gaseous air is fed to the high pressure column 65. Reflux streams (not shown) are sent from the high pressure column to the low pressure column 67 as is well known in the art. In addition, in all modes, gaseous nitrogen 61 is removed from the top of the low pressure column 67 and warmed in exchanger 19 whilst waste nitrogen 59 is removed from lower down the low pressure column 67 and warmed in exchanger 19 before being used to regenerate the purification unit 8.
  • In FIG. 1, all the air is compressed to 15.5 bars in compressor 1 and cooled in cooler 4 to form stream 3. Following further cooling in cooler 6, the air is purified in purification unit 8. The outlet of compressor 1 is connected to the inlet of compressor 5 and to the heat exchanger 19.
  • When the apparatus functions under gas mode, none of the air from compressor 1 is sent to compressor 11 as stream 5. All the air is sent to the warm end of the heat exchange line 19, via open valve 13 as stream 7. The air 7 is cooled to an intermediate temperature of the heat exchange line 19 and is compressed to 26 bars in cold compressor 37. Valve 21 being open, all of the compressed air is then sent back to the heat exchange line 19 via conduit 23, further cooled in conduit 43 and divided in two at an intermediate temperature lower than the inlet temperature of cold compressor 37. One part is cooled completely in the heat exchange line 19 as stream 41, whilst the rest 33 is sent via valve 35 to turbine 39 coupled to cold compressor 37. The expanded air is then sent to a column of the column system. In this example, the air is sent as stream 45 to the high pressure column 65, forming the sole gaseous feed to the high pressure column.
  • In this mode, liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • When the apparatus functions under liquid mode, all the air from compressor 1 is sent to compressors 11, 17 as stream 5 and is compressed to 34 bars, valve 15 being open and valve 13 being closed. The high pressure air 5 is then further compressed to 47 bars in compressor 17 and sent to the warm end of the heat exchange line 19. Once the stream 5 is partially cooled, it is divided in two, one part 41 being cooled completely in the heat exchange line 19 via conduit 43 and the rest 31 being sent to turbine 29 via conduit 23 and valve 21. The expanded air stream 45 is sent to a column of the column system, in this case the high pressure column 65. The compressor 17 is coupled to expander 49 which expands air 47 removed from the high pressure column. The air 51 from the expander 49 is sent to the heat exchange line 19 and warmed therein before being rejected to the atmosphere. Compressor 12 is coupled to expander 29.
  • During this liquid mode, liquid oxygen LOX 53 and liquid nitrogen LIN 69 are removed from the low pressure and high pressure columns respectively. In addition, liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • It will be appreciated that a number of conduits fulfil different purposes depending on which mode is used. The cooling section 43 receives air at 47 bars which is then cooled by passing through the whole heat exchange line during the liquid mode and receives air at 26 bars coming from the cold compressor 37 during the gas mode. In addition, section 28 sees a reversal of flow between the two modes, air flowing in one direction from the heat exchange line 19 to the turbine 29 in liquid mode and in the other direction from the cold compressor 37 to the heat exchange line 19 in gas mode.
  • It will be appreciated that a small amount of liquid may be produced during the gas mode and that gas is produced during the liquid mode.
  • Optionally in all the modes of operation of FIG. 1, the nitrogen 61 is compressed to a higher pressure in compressor 63.
  • In FIG. 2, all the air is compressed to 15.5 bars in compressor 1 and cooled in cooler 4 to form stream 3. Following further cooling in cooler 6, the air is purified in purification unit 8. The outlet of compressor 1 is connected to the inlet of compressor 5 and to the heat exchanger 19.
  • When the apparatus functions under gas mode, none of the air from compressor 1 is sent to compressor 11 as stream 5. All the air is sent to the warm end of the heat exchange line 19, via open valve 13 as stream 7. Valve 15 is closed. The air 7 is cooled to an intermediate temperature of the heat exchange line 19 and is compressed to 26 bars in cold compressor 37. Valve 21 being open, all of the compressed air is then sent back to the heat exchange line 19 via conduit 23, further cooled in conduit 43 and divided in two at an intermediate temperature lower than the inlet temperature of cold compressor 37. One part is cooled completely in the heat exchange line 19 as stream 41, whilst the rest 33 is sent via valve 35 to turbine 39 coupled to cold compressor 37. The expanded air is then sent to a column of the column system. In this example, the air is sent as stream 45 to the high pressure column 65, forming the sole gaseous feed to the high pressure column.
  • In this mode, liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • When the apparatus functions under liquid mode, all the air from compressor 1 is sent to compressors 11,17 as stream 5 and is compressed to 34 bars, valve 15 being open and valve 13 being closed. The high pressure air 5 is then sent to the warm end of the heat exchange line 19. Once the stream 5 is partially cooled, it is divided in two, one part 41 being cooled completely in the heat exchange line 19 via conduit 43 and the rest 31 being sent to turbine 29 via conduit 23 and valve 21. The expanded air stream 45 is sent to a column of the column system, in this case the high pressure column 65. Compressor 17 is coupled to expander 29.
  • During this liquid mode, liquid oxygen LOX 53 and liquid nitrogen LIN 69 are removed from the low pressure and high pressure columns respectively. In addition, liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • It will be appreciated that a number of conduits fulfil different purposes depending on which mode is used. The cooling section 43 receives air which is then cooled by passing through the whole heat exchange line during the liquid mode and receives air at 26 bars coming from the cold compressor 37 during the gas mode. In addition, section 23 sees a reversal of flow between the two modes, air flowing in one direction from the heat exchange line 19 to the turbine 29 in liquid mode and in the other direction from the cold compressor 37 to the heat exchange line 19 in gas mode.
  • It will be appreciated that a small amount of liquid may be produced during the gas mode and that gas is produced during the liquid mode.
  • Optionally in all the modes of operation of FIG. 2, the nitrogen 61 is compressed to a higher pressure in compressor 63.
  • In a simplified version of FIG. 1, as shown in FIG. 3, only two air turbines are used.
  • The process of FIG. 3 may use a double column system as shown and described for FIG. 1, in which a high pressure column 65 is placed underneath a low pressure column 67 and thermally coupled thereto via a reboiler condenser 69.
  • In all the modes of operation, as in the case of FIG. 1, cooled, purified and compressed gaseous air is fed to the high pressure column 65. Reflux streams (not shown) are sent from the high pressure column to the low pressure column 67 as is well known in the art. In addition, in all modes, gaseous nitrogen 61 is removed from the top of the low pressure column 67 and warmed in exchanger 19 whilst waste nitrogen 59 is removed from lower down the low pressure column 67 and warmed in exchanger 19 before being used to regenerate the purification unit 8.
  • In FIG. 3, all the air is compressed to 15.5 bars in compressor 1 and forms stream 3. Following further cooling (not shown), the air is purified in a purification unit (not shown). The outlet of compressor 1 is connected to the inlet of compressor 5 and to the heat exchanger 19.
  • When the apparatus functions under gas mode, none of the air from compressor 1 is sent to compressor 11 as stream 5. All the air is sent to the warm end of the heat exchange line 19, via open valve 13 as stream 7. The air 7 is cooled to an intermediate temperature of the heat exchange line 19 and is compressed to 26 bars in cold compressor 37. Valve 21 being open, all of the compressed air is then sent back to the heat exchange line 19 via conduit 23, further cooled in conduit 43 and divided in two at an intermediate temperature higher than the inlet temperature of cold compressor 37. One part is cooled completely in the heat exchange line 19 as stream 41, whilst the rest 33 is sent via valve 35 to turbine 39 coupled to cold compressor 37. The expanded air is then sent to a column of the column system. In this example, the air is sent as stream 45 to the high pressure column 65, forming the sole gaseous feed to the high pressure column.
  • In this mode, liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • When the apparatus functions under liquid mode, all the air from compressor 1 is sent to compressor 11 as stream 5 and is compressed to 34 bars, valve 15 being open and valve 13 being closed. The high pressure air 5 is then further compressed to 47 bars in compressor 17 and sent to the warm end of the heat exchange line 19. Once the stream 5 is partially cooled, it is divided in two, one part 41 being cooled completely in the heat exchange line 19 via conduit 43 and the rest 31 being sent to turbine 29 via conduit 23. The expanded air stream 45 is sent to a column of the column system, in this case the high pressure column 65. The compressor 17 is coupled to expander 29. During this mode, liquid oxygen LOX 53 and liquid nitrogen LIN 69 are removed from the low pressure and high pressure columns respectively. In addition, liquid oxygen is removed from the bottom of the low pressure column 57 and pressurised as stream 55 in pump 57 before being vaporised in the heat exchanger 19 to form product high pressure gaseous oxygen (HP GOX).
  • It will be appreciated that a number of conduits fulfil different purposes depending on which mode is used. The cooling section 43 receives air at 47 bars which is then cooled by passing through the whole heat exchange line during the liquid mode and receives air at 26 bars coming from the cold compressor 37 during the gas mode. In addition, section 23 sees a reversal of flow between the two modes, air flowing in one direction from the heat exchange line 19 to the turbine 29 in liquid mode and in the other direction from the cold compressor 37 to the heat exchange line 19 in gas mode.
  • For all embodiments, other modes of operation may exist besides the gas mode and liquid mode mentioned.

Claims (12)

1-11. (canceled)
12. A process for the production of at least one liquid product and at least one gaseous product by cryogenic distillation of air under a first mode of operation and a second mode of operation, wherein in all modes of operation the process comprises;
cooling compressed and purified gaseous air in a heat exchange line,
sending said cooled compressed gaseous air to at least one column of a column system,
removing a liquid stream enriched in a component of air from a column of the column system,
vaporizing the removed liquid stream in the heat exchange line,
sending air at an elevated pressure to the heat exchange line, wherein it is condensed and sent to the column system
sending part of the feed air to one of at least two expanders and thereafter to a column of the column system wherein;
a) according to the first mode, the process further comprises,
removing at least part of the feed air from an intermediate point of the heat exchange line,
compressing the removed feed air at a cryogenic temperature in a cold compressor
sending the compressed cryogenic feed air to the heat exchange line to be further cooled,
sending the further cooled compressed cryogenic feed air to the column system,
sending part of the feed air to the first expander; and
b) according to the second mode, the process further comprises,
compressing all of the feed air to a high pressure that is at least 20 bars higher than the highest column pressure of the column system in a second compressor,
cooling the compressed feed air in the heat exchange line,
sending a first part of the cooled compressed feed air to a column system,
sending a second part of the cooled compressed feed air to the second expander, and thereby
producing more liquid as final product during the second mode than during the first mode
13. The process of claim 12, wherein according to the first mode, part of the feed air at the outlet pressure of the cold compressor is cooled and sent to the first expander.
14. The process of claim 12, wherein the cold compressor is coupled to the first expander.
15. The process of claim 12, wherein the second compressor is coupled to the second expander.
16. The process of claim 12, wherein air treated in the second compressor in the second mode and in the cold compressor in the first mode is subsequently sent to a common transfer means upstream of the column system.
17. The process of claim 16, wherein in the first mode the air is sent from the cold compressor to the heat exchange line via a conduit and in the second mode the air is sent from the second compressor to the second expander via the same conduit.
18. The process of claim 16, wherein in the first mode the air is sent from the cold compressor via a passage of the heat exchange line to the cold end thereof and in the second mode the air is sent from the second compressor to the cold end of the heat exchange line via the same passage.
19. An apparatus for the separation of air by cryogenic distillation comprising:
a) a column system,
b) a heat exchange line,
c) a main compressor,
d) a cold compressor connected to the outlet of the main compressor,
e) a second compressor connected to the outlet of the main compressor,
f) first and second expanders,
g) means for sending air from the cold compressor to the first expander,
h) means for sending air from the second compressor to the second expander,
i) means for sending air from the first and second expanders to the column system, and
j) means for sending air from the cold compressor and the second compressor to the column system via the heat exchange means without traversing either of the first and second expanders.
20. The apparatus of claim 19, wherein the means for sending air from the cold compressor to the first expander and means for sending air from the second compressor to the second expander include a common section of conduit.
21. The apparatus of claim 19, wherein the means for sending air from the cold compressor and the second compressor to the column system via the heat exchange means without traversing either of the first and second expanders includes at least one common passage in the heat exchange means.
22. The apparatus of claim 19, further comprising a third expander and means for sending air from the column system to the third expander and thence to the heat exchange means.
US12/671,927 2007-08-10 2007-08-10 Process and Apparatus for the Separation of Air by Cryogenic Distillation Abandoned US20110197630A1 (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10995983B2 (en) * 2014-07-05 2021-05-04 Linde Aktiengesellschaft Method and apparatus for obtaining a compressed gas product by cryogenic separation of air
US20230082208A1 (en) * 2021-09-16 2023-03-16 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Oxygen liquefier design phasing

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2948184B1 (en) 2009-07-20 2016-04-15 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
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
FR2973486B1 (en) * 2011-03-31 2013-05-03 Air Liquide AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION
FR2983287B1 (en) * 2011-11-25 2018-03-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND INSTALLATION OF AIR SEPARATION BY CRYOGENIC DISTILLATION
PL2963370T3 (en) * 2014-07-05 2018-11-30 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5355681A (en) * 1993-09-23 1994-10-18 Air Products And Chemicals, Inc. Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products
US5475980A (en) * 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
US5907959A (en) * 1998-01-22 1999-06-01 Air Products And Chemicals, Inc. Air separation process using warm and cold expanders
US6962062B2 (en) * 2003-12-10 2005-11-08 L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Proédés Georges Claude Process and apparatus for the separation of air by cryogenic distillation
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

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2736543B2 (en) * 1989-04-17 1998-04-02 日本酸素株式会社 Air liquefaction separation method
FR2700205B1 (en) * 1993-01-05 1995-02-10 Air Liquide Method and installation for producing at least one gaseous product under pressure and at least one liquid by air distillation.
FR2703140B1 (en) * 1993-03-23 1995-05-19 Air Liquide Method and installation for producing gaseous oxygen and / or nitrogen gas under pressure by air distillation.
FR2721383B1 (en) * 1994-06-20 1996-07-19 Maurice Grenier Process and installation for producing gaseous oxygen under pressure.
GB9515907D0 (en) * 1995-08-03 1995-10-04 Boc Group Plc Air separation
FR2851330B1 (en) * 2003-02-13 2006-01-06 Air Liquide PROCESS AND PLANT FOR THE PRODUCTION OF A GASEOUS AND HIGH PRESSURE PRODUCTION OF AT LEAST ONE FLUID SELECTED AMONG OXYGEN, ARGON AND NITROGEN BY CRYOGENIC DISTILLATION OF AIR
FR2854683B1 (en) * 2003-05-05 2006-09-29 Air Liquide METHOD AND INSTALLATION FOR PRODUCING PRESSURIZED AIR GASES BY AIR CRYOGENIC DISTILLATION
FR2854682B1 (en) * 2003-05-05 2005-06-17 Air Liquide METHOD AND INSTALLATION OF AIR SEPARATION BY CRYOGENIC DISTILLATION
FR2864214B1 (en) * 2003-12-22 2017-04-21 Air Liquide AIR SEPARATION APPARATUS, INTEGRATED AIR SEPARATION AND METAL PRODUCTION APPARATUS AND METHOD FOR STARTING SUCH AIR SEPARATION APPARATUS
FR2913759B1 (en) * 2007-03-13 2013-08-16 Air Liquide METHOD AND APPARATUS FOR GENERATING GAS AIR FROM THE AIR IN A GAS FORM AND LIQUID WITH HIGH FLEXIBILITY BY CRYOGENIC DISTILLATION

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5355681A (en) * 1993-09-23 1994-10-18 Air Products And Chemicals, Inc. Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products
US5475980A (en) * 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
US5907959A (en) * 1998-01-22 1999-06-01 Air Products And Chemicals, Inc. Air separation process using warm and cold expanders
US6962062B2 (en) * 2003-12-10 2005-11-08 L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Proédés Georges Claude Process and apparatus for the separation of air by cryogenic distillation
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

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10995983B2 (en) * 2014-07-05 2021-05-04 Linde Aktiengesellschaft Method and apparatus for obtaining a compressed gas product by cryogenic separation of air
US20230082208A1 (en) * 2021-09-16 2023-03-16 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Oxygen liquefier design phasing

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CA2695817A1 (en) 2009-02-19
JP2010536003A (en) 2010-11-25
BRPI0721931A2 (en) 2014-03-18
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CN101779092A (en) 2010-07-14

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