WO2009021350A1 - 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
WO2009021350A1
WO2009021350A1 PCT/CN2007/002404 CN2007002404W WO2009021350A1 WO 2009021350 A1 WO2009021350 A1 WO 2009021350A1 CN 2007002404 W CN2007002404 W CN 2007002404W WO 2009021350 A1 WO2009021350 A1 WO 2009021350A1
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WO
WIPO (PCT)
Prior art keywords
air
compressor
sent
heat exchange
mode
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.)
Ceased
Application number
PCT/CN2007/002404
Other languages
French (fr)
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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 Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to JP2010519320A priority Critical patent/JP4908634B2/en
Priority to CN200780100211A priority patent/CN101779092A/en
Priority to US12/671,927 priority patent/US20110197630A1/en
Priority to BRPI0721931-8A priority patent/BRPI0721931A2/en
Priority to PCT/CN2007/002404 priority patent/WO2009021350A1/en
Priority to CA2695817A priority patent/CA2695817A1/en
Priority to EP07785309.1A priority patent/EP2176610B1/en
Publication of WO2009021350A1 publication Critical patent/WO2009021350A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • F25J3/04151—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. 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.
  • 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
  • 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
  • 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
  • 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.
  • 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.
  • Figures 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.
  • 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.
  • the air is sent as stream 45 to the high pressure column 65, forming the sole gaseous feed to the high pressure column.
  • 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. 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.
  • 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).
  • HP GOX product high pressure gaseous oxygen
  • 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.
  • 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).
  • HP GOX product high pressure gaseous oxygen
  • 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.
  • FIG. 3 may use a double column system as shown and described for Figure 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.
  • the air is sent as stream 45 to the high pressure column 65, forming the sole gaseous feed to the high pressure column.
  • 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 for the production of at least one liquid product (53, 71) and at least one gaseous product (55, 61) by cryogenic distillation is disclosed , according to the first mode, at least part of the feed air is removed from an intermediate point of the heat exchange line (19) , compressed at a cryogenic temperature in a cold compressor (37) and sent to the heat exchange line (19) to be further cooled and sent to the column system (65, 67) and part of the feed air is sent to a first expander (39) and 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 (65, 67) in a second compressor (11, 17) , cooled in the heat exchange line (19) and sent in part to a column system (65, 67), another part of the high pressure air being sent to the second expander (29) .

Description

Process and apparatus for the separation of air by cryogenic distillation
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. Figures 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 Figure 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 Figure 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 Figure 1 , the nitrogen 61 is compressed to a higher pressure in compressor 63.
In Figure 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 Figure 2, the nitrogen 61 is compressed to a higher pressure in compressor 63.
In a simplified version of Figure 1 , as shown in Figure 3, only two air turbines are used.
The process of Figure 3 may use a double column system as shown and described for Figure 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 Figure 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 Figure 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

1. Process for the production of at least one liquid product (53) and at least one gaseous product (55,61) 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 (19) and sent to at least one column of a column system (65,67), a liquid stream (55) enriched in a component of air is removed from a column of the column system and vaporised in the heat exchange line, air (3) 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 (29,39) and thence to a column of the column system wherein a) according to the first mode, at least part (7) of the feed air is removed from an intermediate point of the heat exchange line, compressed at a cryogenic temperature in a cold compressor (37) 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 (39) and b) according to the second mode, all of the feed air (5) is compressed to a high pressure at least 20 bars higher than the highest column pressure of the column system in a second compressor (11 ,12,17), 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 (29).
2. Process according to Claim 1 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 (39).
3. Process according to Claim 1 or 2 wherein the cold compressor (37) is coupled to the first expander (39).
4. Process according to Claim 1 ,2 or 3 wherein the second compressor (1 1 ,12,17) is coupled to the second expander (29).
5. Process according to any preceding claim wherein air treated in the second compressor (11 ,12,17) in the second mode and in the cold compressor (37) in the first mode is subsequently sent to a common transfer means (23) upstream of the column system.
6. Process according to Claim 5 wherein in the first mode the air is sent from the cold compressor (37) to the heat exchange line (19) via a conduit (23) and in the second mode the air is sent from the second compressor (11 ,12,17) to the second expander (29) via the same conduit.
7. Process according to Claim 5 wherein in the first mode the air is sent from the cold compressor(37) via a passage of the heat exchange line (19) to the cold end thereof and in the second mode the air is sent from the second compressor (11 ,12,17) to the cold end of the heat exchange line via the same passage.
8. Apparatus for the separation of air by cryogenic distillation comprising: a) a column system (65,67) b) a heat exchange line (19) c) a main compressor (1) d) a cold compressor (37) connected to the outlet of the main compressor e) a second compressor (1 1 ,12,17)connected to the outlet of the main compressor f) first and second expanders (29,39) g) means (21 ,23,43, 33,35) for sending air from the cold compressor to the first expander h) means (21 ,22,23,31) for sending air from the second compressor to the second expander i) means (45,51) for sending air from the first and second expanders to the column system j) means (41) 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.
9. Apparatus according to Claim 8 wherein the means for sending air from the cold compressor (37) to the first expander and means for sending air from the second compressor (11,12) to the second expander (29) include a common section of conduit (23).
10. Apparatus according to Claim 8 wherein the means for sending air from the cold compressor (37) and the second compressor (11 ,12) to the column system via the heat exchange means (19) without traversing either of the first and second expanders (29,39) includes at least one common passage (23) in the heat exchange means.
11. Apparatus according to any of Claims 8 to 10 including a third expander (49) and means for sending air (47) from the column system to the third expander and thence to the heat exchange means (19).
PCT/CN2007/002404 2007-08-10 2007-08-10 Process and apparatus for the separation of air by cryogenic distillation Ceased WO2009021350A1 (en)

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JP2010519320A JP4908634B2 (en) 2007-08-10 2007-08-10 Method and apparatus for separating air by cryogenic distillation
CN200780100211A CN101779092A (en) 2007-08-10 2007-08-10 Method and apparatus for separating air by cryogenic distillation
US12/671,927 US20110197630A1 (en) 2007-08-10 2007-08-10 Process and Apparatus for the Separation of Air by Cryogenic Distillation
BRPI0721931-8A BRPI0721931A2 (en) 2007-08-10 2007-08-10 PROCESS FOR CRYGEN DISTILLATION AIR SEPARATION
PCT/CN2007/002404 WO2009021350A1 (en) 2007-08-10 2007-08-10 Process and apparatus for the separation of air by cryogenic distillation
CA2695817A CA2695817A1 (en) 2007-08-10 2007-08-10 Process and apparatus for the separation of air by cryogenic distillation
EP07785309.1A EP2176610B1 (en) 2007-08-10 2007-08-10 Process for the separation of air by cryogenic distillation

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CN101779092A (en) 2010-07-14
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CA2695817A1 (en) 2009-02-19
BRPI0721931A2 (en) 2014-03-18
JP2010536003A (en) 2010-11-25
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US20110197630A1 (en) 2011-08-18
EP2176610B1 (en) 2019-04-24

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