EP2694898A2 - Method and device for separating air by cryogenic distillation - Google Patents

Method and device for separating air by cryogenic distillation

Info

Publication number
EP2694898A2
EP2694898A2 EP12720248.9A EP12720248A EP2694898A2 EP 2694898 A2 EP2694898 A2 EP 2694898A2 EP 12720248 A EP12720248 A EP 12720248A EP 2694898 A2 EP2694898 A2 EP 2694898A2
Authority
EP
European Patent Office
Prior art keywords
column
oxygen
liquid
air
vaporizer
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP12720248.9A
Other languages
German (de)
French (fr)
Other versions
EP2694898B1 (en
Inventor
Benoit Davidian
Richard Dubettier-Grenier
Loïc JOLY
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
Publication of EP2694898A2 publication Critical patent/EP2694898A2/en
Application granted granted Critical
Publication of EP2694898B1 publication Critical patent/EP2694898B1/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • 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
    • F25J3/0406—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
    • 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
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • F25J3/04309—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • 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
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • the present invention relates to a method and apparatus for air separation by cryogenic distillation.
  • the invention particularly provides a method of producing pure oxygen using a dual vaporizer air separation unit.
  • the method according to the invention allows the production of pure liquid oxygen (containing at least 99 mol%, or even at least 99.6 mol% of oxygen) on an apparatus producing impure oxygen gas (less than 97 mol%, or even 96 mol%) at low pressure, for example in the context of an apparatus for oxycombustion.
  • the oxygen-generating air separation (ASU) schemes for an oxy-fuel coal plant generally comprise two (or three) vaporizers located between the medium pressure column (MP column) and the low pressure column. (BP column).
  • MP column medium pressure column
  • BP column low pressure column
  • the purity of the oxygen produced by this type of plant is typically between 95 and 97 mol%. O 2 .
  • the vaporisation of the oxygen is ensured in a dedicated vaporizer.
  • the vaporization frigories of liquid oxygen are used to condense gaseous air.
  • a method of this kind is known from US-A-4936099 and EP-A-0547946.
  • the pressure of the column MP is so low that it is not possible to use one of the gaseous flows entering or leaving the column MP or the column LP to condense in the bottom vaporizer of the column of Additional pure LOX (their condensing temperature is too low).
  • the invention described here proposes to use as condensing fluid, a fraction of the gaseous air leaving the exchange line and which will subsequently enter the dedicated exchanger ensuring the vaporization of pure oxygen production. (which is referred to as HP air).
  • HP air a fraction of the gaseous air leaving the exchange line and which will subsequently enter the dedicated exchanger ensuring the vaporization of pure oxygen production.
  • This air flow is compressed upstream of the main exchange line by the blower (BAC) of the unit.
  • the pressure of this flow rate is of the order of 4.5 bar abs, higher than that of the MP column, and such that its bubble temperature is higher than the equilibrium temperature of the pure liquid oxygen.
  • the temperature difference between the air flow rate considered and the pure oxygen is of the order of 2 to 3 ° C, a fairly high value, which makes it possible to install a small vaporizer.
  • the production of pure liquid oxygen is free in terms of separation energy and does not play on the separation energy of the production of impure oxygen gas. You just have to pay for the liquefaction energy.
  • the additional refrigeration can be carried out by a liquefaction system independent of the ASU.
  • the invention provides a method for producing pure oxygen (Purity> 99.6%) on a dual vaporizer air separation unit, typically used for oxy-fuel combustion, the majority of which is oxygen produced. at a purity of the order of 95 to 97%. Indeed, on this type of process, apart from HP air, there is no fluid available at sufficiently high condensation temperature to achieve the reboiling of the pure oxygen column.
  • Air separation units are frequently found in a single vaporizer, where a small column producing ultra-pure oxygen is added to the bottom of the LP column.
  • the pressure of the MP column is of the order of 5 to 6 bar and the reboiling of the ultra pure LOX column is provided by a fraction of the flow of gaseous air supplying the MP column.
  • EP-A-0793069 discloses a method according to the preamble of claim 1.
  • air at a first pressure is used to vaporize oxygen in a vaporizer and air at a second pressure, higher than the first one, is used for reboiling a column of pure oxygen.
  • US-A-5916262 discloses a dual purity oxygen production process using an oxygen scrubber heated in tank by air. Pump-pressurized liquid oxygen is also vaporized in the main exchange line by heat exchange with pressurized air.
  • the present invention proposes to produce pure oxygen in a double vaporizer scheme by installing an additional pure oxygen column, the pressure of which is equal to the pressure of the LP column.
  • a method for separating air by cryogenic distillation in a separation unit comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a reboiler vessel and an intermediate reboiler, and a pure oxygen column in which
  • purified air gas is sent and then cooled to a first pressure in an exchange line at the medium pressure column, ii) an oxygen-enriched liquid and a nitrogen-enriched liquid are sent from the medium-pressure column to the low-pressure column,
  • a second flow of oxygen-rich liquid is fed to the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%. oxygen
  • a nitrogen rich gas is withdrawn at the top of the medium pressure column, it is sent to the intermediate reboiler of the low pressure column and the condensed gas is sent to the head of the medium pressure column, and
  • vessel liquid is withdrawn from the pure oxygen column as product and superpressed air is supplied to the second vaporizer pressure to vaporize the first oxygen-rich liquid flow.
  • the first flow of oxygen-rich liquid is pressurized upstream of the vaporizer.
  • the first flow of oxygen-rich liquid and the second flow of oxygen-rich liquid have the same purity.
  • air pressure is divided at the second pressure in two parts, a first portion of superpressed air is sent at the second pressure to the reboiler of the pure oxygen column and a second part of compressed air is sent to the second pressure to the vaporizer.
  • air is sent at the first pressure to the bottom reboiler of the low pressure column to heat it. all the air is divided into a flow at the first pressure and a flow at the second pressure upstream of the exchange line.
  • the first flow of oxygen-rich liquid is less oxygen-rich than the second oxygen-rich flow of oxygen.
  • the first flow of oxygen-rich liquid is vaporized partially in the vaporizer, the formed liquid constituting the second flow of oxygen-rich liquid.
  • the compressed air flow at the second pressure first heats the bottom reboiler of the pure oxygen column and then the vaporizer.
  • Air at the first pressure cools in the exchange line and is sent in gaseous form to the medium pressure column.
  • a cryogenic liquid from an auxiliary source is sent to the double column.
  • medium pressure and low pressure simply mean that the medium pressure column operates at a higher pressure than the low pressure column. These terms are common in the art and clear to those skilled in the art.
  • a cryogenic distillation air separation apparatus comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a bottom reboiler and a reboiler intermediate, and a pure oxygen column, an exchange line, a vaporizer, means for sending purified air gas and then cooled at a first pressure of the exchange line to the medium pressure column, means for supplying an oxygen enriched liquid and a nitrogen enriched liquid from the medium pressure column to the low pressure column, means for withdrawing a nitrogen rich gas from the low pressure column, means for withdrawing an oxygen rich liquid containing at most 97 mol% of oxygen in the tank of the low pressure column, means for sending a first flow of oxygen-rich liquid to the vaporizer, a pipe for sending the gaseous oxygen thus formed to the exchange line, means for sending a second flow of oxygen-rich liquid at the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a
  • a booster a line for sending a superpressed air flow at a second pressure higher than the first pressure to the reboiler of the pure oxygen column, lines for withdrawing a nitrogen-rich gas at the top of the medium pressure column , to send it to the intermediate reboiler of the low pressure column and to send the condensed gas to the head of the medium pressure column and lines to send a nitrogen-rich gas or air to the bottom column reboiler pressure and to send the liquid which condenses thereon to the medium pressure column characterized in that it comprises a pipe for drawing liquid from the column of the pure oxygen column as product and means for sending compressed air at the second pressure of the booster to the vaporizer.
  • the apparatus comprises:
  • the means for sending the supercharged air from the booster to the vaporizer are connected to the bottom reboiler of the pure oxygen column so that the air for the vaporizer passes through the bottom reboiler of the pure oxygen column.
  • the means for sending a second flow of oxygen-rich liquid at the top of the pure oxygen column are constituted by the conduit for sending a bottom liquid from the low pressure column to the top of the pure oxygen column.
  • the vaporizer is not part of a distillation or exhaustion column.
  • a method for separating air by cryogenic distillation in a separation unit comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a reboiler vessel and an intermediate reboiler and a column of pure oxygen in which
  • a second flow of oxygen rich liquid is fed to the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%,
  • a nitrogen rich gas is withdrawn at the top of the medium pressure column, it is sent to the intermediate reboiler of the low pressure column and the condensed gas is sent to the head of the medium pressure column, and
  • a nitrogen-rich gas or air is sent to the bottom reboiler of the low-pressure column and the liquid which condenses therein is sent to the medium-pressure column, characterized in that the liquid from the bottom of the vessel is withdrawn. pure oxygen column as product and in that the first flow of oxygen-rich liquid is less oxygen-rich than the second flow of oxygen-rich liquid.
  • the first flow of oxygen-rich liquid is pressurized upstream of the vaporizer.
  • a second superpressed air flow is sent at the second pressure to the vaporizer.
  • the first flow of oxygen-rich liquid partially vaporizes in the vaporizer, the formed liquid constituting the second flow of oxygen-rich liquid.
  • the supercharged air flow first heats the vessel reboiler of the pure oxygen column and then the vaporizer.
  • a cryogenic liquid from an auxiliary source is sent to the double column.
  • the medium pressure column operates at between 2.5 and 4.5 bar abs.
  • a cryogenic distillation air separation apparatus comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a bottom reboiler and a reboiler intermediate and a pure oxygen column, an exchange line, a vaporizer, means for sending purified air gas and then cooled to a first pressure of the exchange line to the medium pressure column, means for sending an oxygen enriched liquid and a nitrogen enriched liquid from the medium pressure column to the low pressure column, means for withdrawing a nitrogen rich gas from the low pressure column, means for withdrawing an oxygen rich liquid containing at most 97 % mol.
  • a booster a line for sending a superpressed air flow at a second pressure higher than the first tank reboiler pressure of the pure oxygen column, lines for drawing a nitrogen-rich gas at the top of the the medium pressure column, to send it to the intermediate reboiler of the low pressure column and to send the condensed gas to the head of the medium pressure column and lines to send a nitrogen-rich gas or air to the reboiler of the low pressure column and to send the liquid that is condensed in the medium pressure column characterized in that it comprises a pipe for withdrawing liquid from the column of the pure oxygen column as product and a pipe for sending a liquid (53) of the vaporizer (51) at the top pure oxygen column (49).
  • the apparatus may also include a conduit for supplying a bottom liquid from the low pressure column to the top of the pure oxygen column.
  • the means for supplying the blower pressurized air to the vaporizer can be connected to the bottom reboiler of the pure oxygen column so that the air for the vaporizer passes through the bottom reboiler of the pure oxygen column.
  • the means for sending a second flow of oxygen-rich liquid to the top of the pure oxygen column may be constituted by the conduit for sending a bottom liquid from the low pressure column to the top of the pure oxygen column.
  • the apparatus may comprise means for dividing the supercharged air at the second pressure into two parts, the means for supplying superpressed air at the second pressure of the booster to the vaporizer and the duct for sending a pressurized air flow to the booster.
  • the second tank reboiler pressure of the pure oxygen column being connected so that a portion of pressurized air is sent to the bottom reboiler of the pure oxygen column and another portion of pressurized air is sent to the vaporizer.
  • the apparatus may include means for supplying a cryogenic liquid to the low pressure column of an external source.
  • the apparatus may include a conduit for supplying the pressurized air flow from the reboiler of the pure oxygen column to the vaporizer and a conduit for supplying the air from the vaporizer to the medium pressure column and / or the lower column. pressure.
  • the apparatus comprises a pipe for sending the supercharged air flow of the tank reboiler of the pure oxygen column directly to the medium pressure column and / or the low pressure column.
  • the main innovative feature of the invention presented here is that the reboiling of the pure oxygen column is achieved by a fraction of the flow of gaseous air leaving the main exchange line, compressed by a booster at the pressure required for the vaporization of oxygen in the vaporizer (HP air). This fraction of air HP condenses partially or totally in the condenser of the pure oxygen column.
  • the partially condensed compressed air flow possibly after having separated the condensed part (which is then sent into the MP column), is then sent into the product vaporizer where it finishes to condense completely.
  • the partial condensation of the supercharged air allows, with a quasi-nominal flow of GOX production and the same pressure, to operate the vaporizer in pure column vat, then that of the vaporizer produced.
  • the reboiling of the pure liquid oxygen column is therefore free compared to the energy required to vaporize the production.
  • the pressure of this air flow is greater than the pressure of the MP column (typically of the order of 4.5 bar abs against 3.2 bar abs.).
  • Part of the impure liquid is removed from the vaporizer produced (at the same level and instead of the purge of the evaporator), and the pure liquid is sent to the column of oxygen which is a distillation column which is substantially distilled off. same pressure as the vaporizer produces ..
  • the impure gas reflux from the pure oxygen column is mixed with the gas stream from the product vaporizer, the two flows constituting the nominal output flow of the impure GOX.
  • the pure liquid is taken from the vat of the pure oxygen column. It also serves as a purge of deconcentration of the entire device.
  • the addition of frigories can be provided by an independent liquefier, for example by producing liquid nitrogen, from pure nitrogen (from a minaret), which would then be added in liquid form in the apparatus. If there is no pure nitrogen production, it is possible to liquefy residual nitrogen in an independent liquefier.
  • FIG. 1 illustrate air separation methods according to the invention.
  • the air is separated in an ASU comprising a double air separation column, comprising a medium pressure column 23 and a low pressure column 25. Frigories for the separation are provided by expansion of medium pressure nitrogen. in a turbine 47.
  • the apparatus comprises a column of pure liquid oxygen 49, a pump 57, a vaporizer 51 and an exchange line 63.
  • Air 1 is pressurized by a compressor 3 at a pressure between 2.5 and 4.5 bar abs.
  • the air is then purified in a purification unit 5 by adsorption.
  • the air fresh 7 is divided into two parts.
  • Part 9 is overpressed in a booster 13 to a pressure of between 4 and 20 bar abs and then cooled in the exchange line 63 to the cold end.
  • the air 9 is divided into two fractions 15, 17.
  • a fraction 1 5 is sent to the vaporizer 51 where it serves to partially vaporize liquid oxygen comprising at most 97 mol%. oxygen, to produce gaseous oxygen 59 which is heated in the exchange line 63. This gas 59 is sent to an oxyfuel unit.
  • An oxygen-rich liquid 53 is withdrawn from the vaporizer 51 as a purge.
  • the air is condensed.
  • the other fraction of the air 17 is sent to the reboiler 61 of the pure oxygen column 49.
  • This column comprises the reboiler vessel and means for exchanging heat and material above the reboiler.
  • Liquid oxygen 65 comprising at most 97 mol%. oxygen is sent to the top of the column 49 and is enriched to form the liquid product 71 withdrawn into the tank and containing at least 98 mol%. oxygen.
  • the gaseous oxygen at the top of the column 49 is sent to the bottom of the low pressure column 25.
  • the condensed air 17 mixes with the condensed air coming from the vaporizer 51 and, after expansion in a valve 21, is sent to the MP 23 column, which operates at between 2.5 and 4.5 bar abs.
  • Another part 1 1 of the air is cooled in the exchange line 63, is sent to the bottom reboiler 35 of the column BP 25, condenses at least partially and is sent to the bottom of the column MP 23, below the point of arrival of liquid air 19.
  • Oxygen-enriched liquid 27 is withdrawn from the tank of the MP column
  • Low pressure nitrogen 39 is withdrawn at the top of the LP column, reheated in the subcooler 33 and reheated in the exchange line 63.
  • Medium pressure nitrogen 41 is divided in two to form a part
  • the portion 43 serves to heat the intermediate reboiler 37 of the low pressure column 25.
  • the portion 45 is heated in the exchange line 63, is expanded in the turbine 47 and is returned to the line of exchange 63.
  • Liquid oxygen is withdrawn from the tank of the LP column and divided in two.
  • a portion 55 is pressurized in the pump 57 upstream of the vaporizer 51 and the remainder 65 is sent to the top of the pure oxygen column 49 without having been pressurized.
  • the head of the pure oxygen column 49 is therefore at the same pressure as the tank of the low pressure column 25. All or part of the purge liquid 53 can also feed the head of the column 49.
  • a flow of cryogenic liquid 69 for example liquid nitrogen, is sent to the top of the LP column to keep the process cold.
  • the method of FIG. 1 bis differs from that of FIG. 1 in that the column 49 is fed exclusively at the top by the purge 53 of the vaporizer 51, following a step of expansion in a valve.
  • the reboiler 61 of the column 49 is still heated by the pressurized air 17, the air thus condensed being mixed with the pressurized air 15 which was used to heat the vaporizer 51. It is also possible to feed the column with purge liquid 53 and liquid oxygen 65 from the bottom of the low pressure column 25.
  • the method of Figure 2 differs from that of Figure 1 in that the air flow 9 is first sent to the vessel vaporizer 61 of the pure oxygen column 49 and then to the vaporizer 51 where it condenses.
  • the air thus formed is expanded in the valve 21 and sent to the medium pressure column 23.
  • the air fraction 1 1 cools in the exchange line January 1 and is sent to the tank of the medium pressure column 23 without have been relaxed or compressed downstream of the compressor 3.
  • Intermediate reboiler 37 is still heated by medium pressure nitrogen 43 but another part of medium pressure nitrogen 73 is compressed in a cold booster 71 from a cryogenic temperature and sent
  • the condensed nitrogen is expanded in a valve 36 and sent to the top of the MP column 23.
  • the vessel oxygen 55 of the low pressure column is fully pressurized in the pump 57 sent to the vaporizer 51 where it partially vaporizes.
  • the vaporized gas is the gaseous oxygen product 59 containing less than 97 mol%. oxygen.
  • the non-vaporized liquid 53 feeds the top of the column 49.
  • the gaseous oxygen 67 at the top of the column 49 is mixed with the oxygen gas 59.
  • the liquid oxygen 71 constitutes the liquid product. In this case, the pure oxygen column 49 does not operate at the same pressure as the BP column 25.
  • the process of Figure 1 or 1a may use nitrogen to heat the bottom reboiler 35 and the method of Figure 2 may use air to heat the bottom reboiler 35.

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Abstract

The invention relates to a method for separating air by cryogenic distillation in a separation unit including a medium-pressure column (23) and a low-pressure column (25), in which a flow of oxygen-rich liquid is sent to the top of the column of pure oxygen, having a vessel reboiler (61), in which said flow is purified in order to form a vessel liquid containing at least 98 mol % of oxygen and the vessel liquid is drawn off as a product; a supercharged airflow at a second pressure higher than the first pressure is sent to the vessel reboiler of the pure oxygen column and to a liquid oxygen vaporiser (51); a nitrogen-rich gas is drawn from the top of the medium-pressure column; said gas is sent to an intermediate reboiler of the low-pressure column and the condensed gas is sent to the top of the medium-pressure column; and a nitrogen-rich gas or air is sent to a vessel reboiler (36) of the low-pressure column and the liquid that condenses therein is sent to the medium-pressure column.

Description

PROCEDE ET APPAREIL DE SEPARATION D'AIR  METHOD AND APPARATUS FOR AIR SEPARATION
PAR DISTILLATION CRYOGENIQUE La présente invention est relative à un procédé et à un appareil de séparation d'air par distillation cryogénique.  The present invention relates to a method and apparatus for air separation by cryogenic distillation.
L'invention propose en particulier une méthode de production d'oxygène pur utilisant une unité de séparation d'air à double vaporiseur.  The invention particularly provides a method of producing pure oxygen using a dual vaporizer air separation unit.
Le procédé selon l'invention permet la production d'oxygène liquide pur (contenant au moins 99% mol., voire au moins 99,6% mol. d'oxygène) sur un appareil produisant de l'oxygène gazeux impur (inférieur à 97% mol., voire à 96% mol.) à faible pression, par exemple dans le cadre d'un appareil pour l'oxycombustion.  The method according to the invention allows the production of pure liquid oxygen (containing at least 99 mol%, or even at least 99.6 mol% of oxygen) on an apparatus producing impure oxygen gas (less than 97 mol%, or even 96 mol%) at low pressure, for example in the context of an apparatus for oxycombustion.
Les schémas d'un ités de séparation d'air (ASU) produisant l'oxygène destiné à une centrale à charbon à oxycombustion comprennent en général deux vaporiseurs (voire trois) situés entre la colonne moyenne pression (colonne MP) et la colonne basse pression (colonne BP). L'installation de ces deux vaporiseurs permet de réduire la pression de la colonne MP jusqu'à une valeur de l'ordre de 3 bar absolus, ce qui permet de minimiser la consommation énergétique de l'ASU.  The oxygen-generating air separation (ASU) schemes for an oxy-fuel coal plant generally comprise two (or three) vaporizers located between the medium pressure column (MP column) and the low pressure column. (BP column). The installation of these two vaporizers makes it possible to reduce the pressure of the MP column up to a value of the order of 3 bar absolute, which makes it possible to minimize the energy consumption of the ASU.
La pureté de l'oxygène produit par ce type de centrale est typiquement comprise entre 95 et 97% mol. O2. La vaporisation de l'oxygène est assurée dans un vaporiseur dédié. Les frigories de vaporisation de l'oxygène liquide sont utilisées pour condenser de l'air gazeux. Un procédé de ce genre est connu de US-A-4936099 et de EP-A-0547946. The purity of the oxygen produced by this type of plant is typically between 95 and 97 mol%. O 2 . The vaporisation of the oxygen is ensured in a dedicated vaporizer. The vaporization frigories of liquid oxygen are used to condense gaseous air. A method of this kind is known from US-A-4936099 and EP-A-0547946.
Par ailleurs, on peut tenter de profiter de l'installation d'un tel ASU pour produire de l'azote liquide pur et de l'oxygène pur (pureté de l'ordre de 99,6%), stockés puis destinés au commerce liquide par camions.  Moreover, one can try to take advantage of the installation of such an ASU to produce pure liquid nitrogen and pure oxygen (purity of the order of 99.6%), stored and then intended for liquid trade by trucks.
La production d'azote liquide ne pose pas de difficulté majeure, car il suffit de rajouter des plateaux en haut de la colonne MP pour atteindre la pureté désirée, sans impact sur le reste du procédé de l'ASU, à part le coût de l'énergie de liquéfaction.  The production of liquid nitrogen poses no major difficulty, because it is sufficient to add trays at the top of the MP column to achieve the desired purity, without impact on the rest of the ASU process, apart from the cost of liquefaction energy.
En revanche, la production d'oxygène pur (> 99,6%) induit un impact plus important sur le procédé ; en effet, la pureté du liquide produit est nettement supérieure à celle de l'oxygène gazeux livré à la centrale à oxycombustion. Il est donc nécessaire d'installer une petite colonne supplémentaire, récupérant une fraction du débit liquide recueilli dans la colonne BP (en cuve ou à un plateau intermédiaire), le distillant, ce qui permet de récupérer en bas de cette petite colonne additionnelle l'oxygène pur destiné au commerce par camions. Le retour gazeux depuis la colonne de LOX pur s'effectue alors au même niveau que le piquage de liquide dans la colonne BP. On the other hand, the production of pure oxygen (> 99.6%) induces a greater impact on the process; indeed, the purity of the liquid produced is clearly higher than that of the oxygen gas delivered to the oxy-fuel power station. It is therefore necessary to install a small additional column, recovering a fraction of the liquid flow collected in the LP column (in the tank or on an intermediate plateau), distilling it, which makes it possible to recover at the bottom of this small additional column. pure oxygen for trade by trucks. The gas return from the pure LOX column is then performed at the same level as the liquid tapping in the LP column.
Néanmoins, la pression de la colonne MP est tellement basse qu'il n'est pas possible d'utiliser un des débits gazeux entrant ou sortant de la colonne MP ni de la colonne BP pour se condenser dans le vaporiseur de cuve de la colonne de LOX pure additionnelle (leur température de condensation est trop basse).  Nevertheless, the pressure of the column MP is so low that it is not possible to use one of the gaseous flows entering or leaving the column MP or the column LP to condense in the bottom vaporizer of the column of Additional pure LOX (their condensing temperature is too low).
L'invention décrite ici propose d'utiliser comme fluide se condensant, une fraction de l'air gazeux sortant de la ligne d'échange et qui va par la suite entrer dans l'échangeur dédié assurant la vaporisation de la production d'oxygène pur (qu'on désigne par le terme d'air HP). Ce débit d'air est comprimé en amont de la ligne d'échange principale par le surpresseur (BAC) de l'unité.  The invention described here proposes to use as condensing fluid, a fraction of the gaseous air leaving the exchange line and which will subsequently enter the dedicated exchanger ensuring the vaporization of pure oxygen production. (which is referred to as HP air). This air flow is compressed upstream of the main exchange line by the blower (BAC) of the unit.
La pression de ce débit est de l'ordre de 4,5 bars abs, supérieure à celle de la colonne MP, et telle que sa température de bulle soit supérieure à la température d'équilibre de l'oxygène liquide pur.  The pressure of this flow rate is of the order of 4.5 bar abs, higher than that of the MP column, and such that its bubble temperature is higher than the equilibrium temperature of the pure liquid oxygen.
L'écart de température entre le débit d'air considéré et l'oxygène pur est de l'ordre de 2 à 3°C, valeur assez élevée, ce qui permet d'installer un vaporiseur de petite taille.  The temperature difference between the air flow rate considered and the pure oxygen is of the order of 2 to 3 ° C, a fairly high value, which makes it possible to install a small vaporizer.
Dans l'invention, selon la variante de la Figure 1 , la production d'oxygène liquide pur est gratuite en termes d'énergie de séparation et ne joue pas sur l'énergie de séparation de la production de l'oxygène gazeux impur. Il faut juste payer l'énergie de liquéfaction. L'appoint frigorifique peut être effectué par un système de liquéfaction indépendant de l'ASU.  In the invention, according to the variant of Figure 1, the production of pure liquid oxygen is free in terms of separation energy and does not play on the separation energy of the production of impure oxygen gas. You just have to pay for the liquefaction energy. The additional refrigeration can be carried out by a liquefaction system independent of the ASU.
L'invention propose une méthode permettant de produire de l'oxygène pur (Pureté > 99,6%) sur une unité de séparation d'air à double vaporiseur, typiquement utilisée pour l'oxycombustion, dont la majorité de l'oxygène est produite à une pureté de l'ordre de 95 à 97%. En effet, sur ce type de procédé, hormis l'air HP, il n'existe pas de fluide disponible à température de condensation suffisamment haute pour réaliser le rebouillage de la colonne d'oxygène pur. The invention provides a method for producing pure oxygen (Purity> 99.6%) on a dual vaporizer air separation unit, typically used for oxy-fuel combustion, the majority of which is oxygen produced. at a purity of the order of 95 to 97%. Indeed, on this type of process, apart from HP air, there is no fluid available at sufficiently high condensation temperature to achieve the reboiling of the pure oxygen column.
A l'heure actuelle, il n'existe pas de solution référencée pour produire de l'oxygène pur sur une unité de séparation d'air à double vaporiseur.  At present, there is no referenced solution for producing pure oxygen on a dual vaporizer air separation unit.
On pourrait utiliser, dans ce but, un débit soutiré à un niveau intermédiaire (et donc à température plus élevée) dans la ligne d'échange principale, mais ceci complexifierait le procédé. Ce serait également moins efficace car il s'agirait d'utiliser de la chaleur sensible contre de la chaleur latente.  For this purpose, a flow drawn off at an intermediate level (and therefore at a higher temperature) could be used in the main exchange line, but this would complicate the process. It would also be less effective because it would involve using sensible heat against latent heat.
On trouve fréquemment des unités de séparation d'air (ASU) à un seul vaporiseur, où une petite colonne produisant de production l'oxygène ultra-pur est rajoutée en cuve de la colonne BP. Dans ce cas, la pression de la colonne MP est de l'ordre de 5 à 6 bars et le rebouillage de la colonne de LOX ultra pur est assuré par une fraction du débit d'air gazeux alimentant la colonne MP.  Air separation units (ASU) are frequently found in a single vaporizer, where a small column producing ultra-pure oxygen is added to the bottom of the LP column. In this case, the pressure of the MP column is of the order of 5 to 6 bar and the reboiling of the ultra pure LOX column is provided by a fraction of the flow of gaseous air supplying the MP column.
EP-A-0793069 décrit un procédé selon le préambule de la revendication 1 . EP-A-0793069 discloses a method according to the preamble of claim 1.
Selon ce procédé, de l'air à une première pression est utilisé pour vaporiser de l'oxygène dans un vaporiseur et de l'air à une deuxième pression, plus élevée que la première, est utilisée pour le rebouillage d'une colonne d'oxygène pur. According to this method, air at a first pressure is used to vaporize oxygen in a vaporizer and air at a second pressure, higher than the first one, is used for reboiling a column of pure oxygen.
US-A-5916262 décrit un procédé de production d'oxygène à deux puretés, utilisant une colonne d'épuration d'oxygène chauffé en cuve par de l'air. De l'oxygène liquide pressurisé par pompe est également vaporisé dans la ligne d'échange principale par échange de chaleur avec de l'air surpressé.  US-A-5916262 discloses a dual purity oxygen production process using an oxygen scrubber heated in tank by air. Pump-pressurized liquid oxygen is also vaporized in the main exchange line by heat exchange with pressurized air.
La présente invention propose de produire de l'oxygène pur sur un schéma à double vaporiseur en installant une colonne d'oxygène pur supplémentaire, dont la pression est égale à la pression de la colonne BP.  The present invention proposes to produce pure oxygen in a double vaporizer scheme by installing an additional pure oxygen column, the pressure of which is equal to the pressure of the LP column.
Selon un objet de l'invention, il est prévu, un procédé de séparation d'air par distillation cryogénique dans une unité de séparation comprenant une colonne moyenne pression et une colonne basse pression, reliées thermiquement entre elles, la colonne basse pression comprenant un rebouilleur de cuve et un rebouilleur intermédiaire, et une colonne d'oxygène pur dans lequel  According to an object of the invention, there is provided a method for separating air by cryogenic distillation in a separation unit comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a reboiler vessel and an intermediate reboiler, and a pure oxygen column in which
i) on envoie de l'air gazeux épuré puis refroidi à une première pression dans une ligne d'échange à la colonne moyenne pression, ii) on envoie un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, i) purified air gas is sent and then cooled to a first pressure in an exchange line at the medium pressure column, ii) an oxygen-enriched liquid and a nitrogen-enriched liquid are sent from the medium-pressure column to the low-pressure column,
iii) on soutire un gaz riche en azote de la colonne basse pression, iv) on soutire un liquide riche en oxygène contenant au plus 97% mol. d'oxygène en cuve de la colonne basse pression,  iii) a nitrogen rich gas is withdrawn from the low pressure column, iv) an oxygen-rich liquid containing at most 97 mol% is withdrawn. of oxygen in the tank of the low pressure column,
v) on envoie un premier débit de liquide riche en oxygène à un vaporiseur et on envoie l'oxygène gazeux ainsi formé à la ligne d'échange,  v) a first flow of oxygen-rich liquid is sent to a vaporizer and the gaseous oxygen thus formed is sent to the exchange line,
vi) on envoie un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur, ayant un rebouilleur de cuve , où il s'épure pour former un liquide de cuve contenant au moins 98% mol. d'oxygène,  vi) a second flow of oxygen-rich liquid is fed to the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%. oxygen,
vii) on envoie un débit d'air surpressé à une deuxième pression supérieure à la première pression au rebouilleur de cuve de la colonne d'oxygène pur,  vii) a superpressed air flow is sent at a second pressure higher than the first tank reboiler pressure of the pure oxygen column,
viii) on soutire un gaz riche en azote en tête de la colonne moyenne pression, on l'envoie au rebouilleur intermédiaire de la colonne basse pression et on envoie le gaz condensé à la tête de la colonne moyenne pression, et  viii) a nitrogen rich gas is withdrawn at the top of the medium pressure column, it is sent to the intermediate reboiler of the low pressure column and the condensed gas is sent to the head of the medium pressure column, and
ix) on envoie un gaz riche en azote ou de l'air au rebouilleur de cuve de la colonne basse pression et on envoie le liquide qui s'y condense à la colonne moyenne pression  ix) a nitrogen-rich gas or air is sent to the bottom reboiler of the low pressure column and the liquid which is condensed therein is sent to the medium pressure column
caractérisé en ce que l'on soutire du liquide de cuve de la colonne d'oxygène pur comme produit et en ce que l'on envoie de l'air surpressé à la deuxième pression au vaporiseur pour vaporiser le premier débit de liquide riche en oxygène.  characterized in that vessel liquid is withdrawn from the pure oxygen column as product and superpressed air is supplied to the second vaporizer pressure to vaporize the first oxygen-rich liquid flow. .
Selon d'autres aspects facultatifs de l'invention :  According to other optional aspects of the invention:
on pressurise le premier débit de liquide riche en oxygène en amont du vaporiseur.  the first flow of oxygen-rich liquid is pressurized upstream of the vaporizer.
le premier débit de liquide riche en oxygène et le deuxième débit de liquide riche en oxygène ont la même pureté.  the first flow of oxygen-rich liquid and the second flow of oxygen-rich liquid have the same purity.
on divise de l'air surpressé à la deuxième pression en deux parties, on envoie une première partie d'air surpressé à la deuxième pression au rebouilleur de cuve de la colonne d'oxygène pur et on envoie une deuxième partie d'air surpressé à la deuxième pression au vaporiseur.  air pressure is divided at the second pressure in two parts, a first portion of superpressed air is sent at the second pressure to the reboiler of the pure oxygen column and a second part of compressed air is sent to the second pressure to the vaporizer.
on envoie de l'air à la première pression au rebouilleur de cuve de la colonne basse pression pour le chauffer. tout l'air est divisé en un débit à la première pression et un débit à la deuxième pression en amont de la ligne d'échange. air is sent at the first pressure to the bottom reboiler of the low pressure column to heat it. all the air is divided into a flow at the first pressure and a flow at the second pressure upstream of the exchange line.
le premier débit de liquide riche en oxygène est moins riche en oxygène que le deuxième débit de liquide riche en oxygène.  the first flow of oxygen-rich liquid is less oxygen-rich than the second oxygen-rich flow of oxygen.
- le premier débit de liquide riche en oxygène se vaporise partiellement dans le vaporiseur, le liquide formé constituant le deuxième débit de liquide riche en oxygène.  - The first flow of oxygen-rich liquid is vaporized partially in the vaporizer, the formed liquid constituting the second flow of oxygen-rich liquid.
le débit d'air surpressé à la deuxième pression chauffe d'abord le rebouilleur de cuve de la colonne d'oxygène pur et ensuite le vaporiseur.  the compressed air flow at the second pressure first heats the bottom reboiler of the pure oxygen column and then the vaporizer.
- de l'air à la première pression se refroidit dans la ligne d'échange et est envoyé sous forme gazeuse à la colonne moyenne pression.  - Air at the first pressure cools in the exchange line and is sent in gaseous form to the medium pressure column.
un liquide cryogénique d'une source auxiliaire est envoyé à la double colonne.  a cryogenic liquid from an auxiliary source is sent to the double column.
Les termes « moyenne pression » et « basse pression » désignent simplement que la colonne moyenne pression opère à une pression plus élevée que la colonne basse pression. Ces termes sont communs dans l'art et clairs pour l'homme de l'art.  The terms "medium pressure" and "low pressure" simply mean that the medium pressure column operates at a higher pressure than the low pressure column. These terms are common in the art and clear to those skilled in the art.
Selon un autre objet de l'invention, il est prévu un appareil de séparation d'air par distillation cryogénique comprenant une colonne moyenne pression et une colonne basse pression, reliées thermiquement entre elles, la colonne basse pression comprenant un rebouilleur de cuve et un rebouilleur intermédiaire, et une colonne d'oxygène pur, une ligne d'échange , un vaporiseur , des moyens pour envoyer de l'air gazeux épuré puis refroidi à une première pression de la ligne d'échange à la colonne moyenne pression, des moyens pour envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, des moyens pour soutirer un gaz riche en azote de la colonne basse pression, des moyens pour soutirer un liquide riche en oxygène contenant au plus 97% mol. d'oxygène en cuve de la colonne basse pression, des moyens pour envoyer un premier débit de liquide riche en oxygène au vaporiseur, une conduite pour envoyer l'oxygène gazeux ainsi formé à la ligne d'échange, des moyens pour envoyer un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur, ayant un rebouilleur de cuve, où il s'épure pour former un liquide de cuve contenant au moins 98% mol. d'oxygène, un surpresseur, une conduite pour envoyer un débit d'air surpressé à une deuxième pression supérieure à la première pression au rebouilleur de cuve de la colonne d'oxygène pur, des conduites pour soutirer un gaz riche en azote en tête de la colonne moyenne pression, pour l'envoyer au rebouilleur intermédiaire de la colonne basse pression et pour envoyer le gaz condensé à la tête de la colonne moyenne pression et des conduites pour envoyer un gaz riche en azote ou de l'air au rebouilleur de cuve de la colonne basse pression et pour envoyer le liquide qui s'y condense à la colonne moyenne pression caractérisé en ce qu'il comprend une conduite pour soutirer du liquide de cuve de la colonne d'oxygène pur comme produit et des moyens pour envoyer de l'air surpressé à la deuxième pression du surpresseur au vaporiseur. According to another object of the invention, there is provided a cryogenic distillation air separation apparatus comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a bottom reboiler and a reboiler intermediate, and a pure oxygen column, an exchange line, a vaporizer, means for sending purified air gas and then cooled at a first pressure of the exchange line to the medium pressure column, means for supplying an oxygen enriched liquid and a nitrogen enriched liquid from the medium pressure column to the low pressure column, means for withdrawing a nitrogen rich gas from the low pressure column, means for withdrawing an oxygen rich liquid containing at most 97 mol% of oxygen in the tank of the low pressure column, means for sending a first flow of oxygen-rich liquid to the vaporizer, a pipe for sending the gaseous oxygen thus formed to the exchange line, means for sending a second flow of oxygen-rich liquid at the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%. oxygen, a booster, a line for sending a superpressed air flow at a second pressure higher than the first pressure to the reboiler of the pure oxygen column, lines for withdrawing a nitrogen-rich gas at the top of the medium pressure column , to send it to the intermediate reboiler of the low pressure column and to send the condensed gas to the head of the medium pressure column and lines to send a nitrogen-rich gas or air to the bottom column reboiler pressure and to send the liquid which condenses thereon to the medium pressure column characterized in that it comprises a pipe for drawing liquid from the column of the pure oxygen column as product and means for sending compressed air at the second pressure of the booster to the vaporizer.
Selon d'autres objets facultatifs de l'invention, il est prévu que l'appareil comprenne :  According to other optional objects of the invention, it is provided that the apparatus comprises:
une conduite pour envoyer un liquide du vaporiseur en tête de la colonne d'oxygène pur et/ou  a pipe for sending a liquid from the vaporizer to the top of the pure oxygen column and / or
une conduite pour envoyer un liquide de cuve de la colonne basse pression en tête de la colonne d'oxygène pur  a pipe to send a bottom liquid from the low pressure column to the top of the pure oxygen column
les moyens pour envoyer l'air surpressé du surpresseur au vaporiseur sont reliés au rebouilleur de cuve de la colonne d'oxygène pur de sorte que l'air destiné au vaporiseur passe à travers le rebouilleur de cuve de la colonne d'oxygène pur.  the means for sending the supercharged air from the booster to the vaporizer are connected to the bottom reboiler of the pure oxygen column so that the air for the vaporizer passes through the bottom reboiler of the pure oxygen column.
les moyens pour envoyer un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur sont constitués par la conduite pour envoyer un liquide de cuve de la colonne basse pression en tête de la colonne d'oxygène pur.  the means for sending a second flow of oxygen-rich liquid at the top of the pure oxygen column are constituted by the conduit for sending a bottom liquid from the low pressure column to the top of the pure oxygen column.
des moyens pour diviser l'air surpressé à la deuxième pression en deux parties, les moyens pour envoyer de l'air surpressé à la deuxième pression du surpresseur au vaporiseur et la conduite pour envoyer un débit d'air surpressé à la deuxième pression au rebouilleur de cuve de la colonne d'oxygène pur étant reliés de sorte qu'une partie d'air surpressé est envoyée au rebouilleur de cuve de la colonne d'oxygène pur et une autre partie d'air surpressé est envoyée au vaporiseur. Le vaporiseur ne fait pas partie d'une colonne de distillation ou d'épuisement. means for dividing the supercharged air at the second pressure into two parts, the means for supplying superpressurized air at the second pressure of the booster to the vaporizer and the duct for sending a superpressed air flow to the second reboiler pressure the vessel of the pure oxygen column being connected so that a portion of pressurized air is sent to the bottom reboiler of the pure oxygen column and another portion of pressurized air is sent to the vaporizer. The vaporizer is not part of a distillation or exhaustion column.
Selon un autre objet de l'invention, il est prévu un procédé de séparation d'air par distillation cryogénique dans une unité de séparation comprenant une colonne moyenne pression et une colonne basse pression, reliées thermiquement entre elles, la colonne basse pression comprenant un rebouilleur de cuve et un rebouilleur intermédiaire et une colonne d'oxygène pur dans lequel  According to another object of the invention, there is provided a method for separating air by cryogenic distillation in a separation unit comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a reboiler vessel and an intermediate reboiler and a column of pure oxygen in which
i) on envoie de l'air gazeux épuré puis refroidi à une première pression dans une ligne d'échange à la colonne moyenne pression,  i) purified air gas is sent and then cooled to a first pressure in an exchange line at the medium pressure column,
ii) on envoie un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression,  ii) an oxygen-enriched liquid and a nitrogen-enriched liquid are sent from the medium-pressure column to the low-pressure column,
iii) on soutire un gaz riche en azote de la colonne basse pression, iv) on soutire un liquide riche en oxygène contenant au plus 97% mol. d'oxygène en cuve de la colonne basse pression,  iii) a nitrogen rich gas is withdrawn from the low pressure column, iv) an oxygen-rich liquid containing at most 97 mol% is withdrawn. of oxygen in the tank of the low pressure column,
v) on envoie un premier débit de liquide riche en oxygène à un vaporiseur et on envoie l'oxygène gazeux ainsi formé à la ligne d'échange,  v) a first flow of oxygen-rich liquid is sent to a vaporizer and the gaseous oxygen thus formed is sent to the exchange line,
vi) on envoie un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur, ayant un rebouilleur de cuve, où il s'épure pour former un liquide de cuve contenant au moins 98% mol.,  vi) a second flow of oxygen rich liquid is fed to the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%,
vii) on envoie un débit d'air surpressé à une deuxième pression supérieure à la première pression au rebouilleur de cuve de la colonne d'oxygène pur,  vii) a superpressed air flow is sent at a second pressure higher than the first tank reboiler pressure of the pure oxygen column,
viii) on soutire un gaz riche en azote en tête de la colonne moyenne pression, on l'envoie au rebouilleur intermédiaire de la colonne basse pression et on envoie le gaz condensé à la tête de la colonne moyenne pression, et  viii) a nitrogen rich gas is withdrawn at the top of the medium pressure column, it is sent to the intermediate reboiler of the low pressure column and the condensed gas is sent to the head of the medium pressure column, and
ix) on envoie un gaz riche en azote ou de l'air au rebouilleur de cuve de la colonne basse pression et on envoie le liquide qui s'y condense à la colonne moyenne pression caractérisé en ce que on soutire du liquide de cuve de la colonne d'oxygène pur comme produit et en ce que le premier débit de liquide riche en oxygène est moins riche en oxygène que le deuxième débit de liquide riche en oxygène.  ix) a nitrogen-rich gas or air is sent to the bottom reboiler of the low-pressure column and the liquid which condenses therein is sent to the medium-pressure column, characterized in that the liquid from the bottom of the vessel is withdrawn. pure oxygen column as product and in that the first flow of oxygen-rich liquid is less oxygen-rich than the second flow of oxygen-rich liquid.
Selon d'autres caractéristiques facultatives :  According to other optional features:
on pressurise le premier débit de liquide riche en oxygène en amont du vaporiseur. - on envoie un deuxième débit d'air surpressé à la deuxième pression au vaporiseur. the first flow of oxygen-rich liquid is pressurized upstream of the vaporizer. a second superpressed air flow is sent at the second pressure to the vaporizer.
le premier débit de liquide riche en oxygène se vaporise partiellement dans le vaporiseur, le liquide formé constituant le deuxième débit de liquide riche en oxygène.  the first flow of oxygen-rich liquid partially vaporizes in the vaporizer, the formed liquid constituting the second flow of oxygen-rich liquid.
le débit d'air surpressé chauffe d'abord le rebouilleur de cuve de la colonne d'oxygène pur et ensuite le vaporiseur.  the supercharged air flow first heats the vessel reboiler of the pure oxygen column and then the vaporizer.
un liquide cryogénique d'une source auxiliaire est envoyé à la double colonne.  a cryogenic liquid from an auxiliary source is sent to the double column.
- la colonne moyenne pression opère à entre 2,5 et 4,5 bars abs.  the medium pressure column operates at between 2.5 and 4.5 bar abs.
Selon un autre objet de l'invention, il est prévu un appareil de séparation d'air par distillation cryogénique comprenant une colonne moyenne pression et une colonne basse pression, reliées thermiquement entre elles, la colonne basse pression comprenant un rebouilleur de cuve et un rebouilleur intermédiaire et une colonne d'oxygène pur, une ligne d'échange, un vaporiseur, des moyens pour envoyer de l'air gazeux épuré puis refroidi à une première pression de la ligne d'échange à la colonne moyenne pression, des moyens pour envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, des moyens pour soutirer un gaz riche en azote de la colonne basse pression, des moyens pour soutirer un liquide riche en oxygène contenant au plus 97% mol. d'oxygène en cuve de la colonne basse pression, des moyens pour envoyer un premier débit de liquide riche en oxygène au vaporiseur, une conduite pour envoyer l'oxygène gazeux ainsi formé à la ligne d'échange, des moyens pour envoyer un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur, ayant un rebouilleur de cuve , où il s'épure pour former un liquide de cuve contenant au moins 98% mol. d'oxygène, un surpresseur, une conduite pour envoyer un débit d'air surpressé à une deuxième pression supérieure à la première pression au rebouilleur de cuve de la colonne d'oxygène pur, des conduites pour soutirer un gaz riche en azote en tête de la colonne moyenne pression, pour l'envoyer au rebouilleur intermédiaire de la colonne basse pression et pour envoyer le gaz condensé à la tête de la colonne moyenne pression et des conduites pour envoyer un gaz riche en azote ou de l'air au rebouilleur de cuve de la colonne basse pression et pour envoyer le liquide qui s'y condense à la colonne moyenne pression caractérisé en ce qu'il comprend une conduite pour soutirer du liquide de cuve de la colonne d'oxygène pur comme produit et une conduite pour envoyer un liquide (53) du vaporiseur (51 ) en tête de la colonne d'oxygène pur (49). According to another object of the invention, there is provided a cryogenic distillation air separation apparatus comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a bottom reboiler and a reboiler intermediate and a pure oxygen column, an exchange line, a vaporizer, means for sending purified air gas and then cooled to a first pressure of the exchange line to the medium pressure column, means for sending an oxygen enriched liquid and a nitrogen enriched liquid from the medium pressure column to the low pressure column, means for withdrawing a nitrogen rich gas from the low pressure column, means for withdrawing an oxygen rich liquid containing at most 97 % mol. of oxygen in the tank of the low pressure column, means for sending a first flow of oxygen-rich liquid to the vaporizer, a pipe for sending the gaseous oxygen thus formed to the exchange line, means for sending a second flow of oxygen-rich liquid at the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%. of oxygen, a booster, a line for sending a superpressed air flow at a second pressure higher than the first tank reboiler pressure of the pure oxygen column, lines for drawing a nitrogen-rich gas at the top of the the medium pressure column, to send it to the intermediate reboiler of the low pressure column and to send the condensed gas to the head of the medium pressure column and lines to send a nitrogen-rich gas or air to the reboiler of the low pressure column and to send the liquid that is condensed in the medium pressure column characterized in that it comprises a pipe for withdrawing liquid from the column of the pure oxygen column as product and a pipe for sending a liquid (53) of the vaporizer (51) at the top pure oxygen column (49).
L'appareil peut également comprendre une conduite pour envoyer un liquide de cuve de la colonne basse pression en tête de la colonne d'oxygène pur.  The apparatus may also include a conduit for supplying a bottom liquid from the low pressure column to the top of the pure oxygen column.
Les moyens pour envoyer l'air surpressé du surpresseur au vaporiseur peuvent être reliés au rebouilleur de cuve de la colonne d'oxygène pur de sorte que l'air destiné au vaporiseur passe à travers le rebouilleur de cuve de la colonne d'oxygène pur.  The means for supplying the blower pressurized air to the vaporizer can be connected to the bottom reboiler of the pure oxygen column so that the air for the vaporizer passes through the bottom reboiler of the pure oxygen column.
Les moyens pour envoyer un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur peuvent être constitués par la conduite pour envoyer un liquide de cuve de la colonne basse pression en tête de la colonne d'oxygène pur.  The means for sending a second flow of oxygen-rich liquid to the top of the pure oxygen column may be constituted by the conduit for sending a bottom liquid from the low pressure column to the top of the pure oxygen column.
L'appareil peut comprendre des moyens pour diviser l'air surpressé à la deuxième pression en deux parties, les moyens pour envoyer de l'air surpressé à la deuxième pression du surpresseur au vaporiseur et la conduite pour envoyer un débit d'air surpressé à la deuxième pression au rebouilleur de cuve de la colonne d'oxygène pur étant reliés de sorte qu'une partie d'air surpressé est envoyée au rebouilleur de cuve de la colonne d'oxygène pur et une autre partie d'air surpressé est envoyée au vaporiseur.  The apparatus may comprise means for dividing the supercharged air at the second pressure into two parts, the means for supplying superpressed air at the second pressure of the booster to the vaporizer and the duct for sending a pressurized air flow to the booster. the second tank reboiler pressure of the pure oxygen column being connected so that a portion of pressurized air is sent to the bottom reboiler of the pure oxygen column and another portion of pressurized air is sent to the vaporizer.
L'appareil peut comprendre des moyens pour envoyer un liquide cryogénique à la colonne basse pression d'une source extérieure.  The apparatus may include means for supplying a cryogenic liquid to the low pressure column of an external source.
L'appareil peut comprendre une conduite pour envoyer le débit d'air surpressé du rebouilleur de cuve de la colonne d'oxygène pur au vaporiseur et une conduite pour envoyer l'air du vaporiseur à la colonne moyenne pression et/ou à la colonne basse pression.  The apparatus may include a conduit for supplying the pressurized air flow from the reboiler of the pure oxygen column to the vaporizer and a conduit for supplying the air from the vaporizer to the medium pressure column and / or the lower column. pressure.
Selon une autre variante l'appareil comprend une conduite pour envoyer le débit d'air surpressé du rebouilleur de cuve de la colonne d'oxygène pur directement à la colonne moyenne pression et/ou à la colonne basse pression.  According to another variant the apparatus comprises a pipe for sending the supercharged air flow of the tank reboiler of the pure oxygen column directly to the medium pressure column and / or the low pressure column.
La principale caractéristique innovante de l'invention présentée ici est que le rebouillage de la colonne d'oxygène pur est réalisé par une fraction du débit d'air gazeux sortant de la ligne d'échange principale, comprimée par un surpresseur à la pression requise pour la vaporisation d'oxygène dans le vaporiseur (air HP). Cette fraction d'air HP se condense partiellement ou totalement dans le condenseur de la colonne d'oxygène pur. The main innovative feature of the invention presented here is that the reboiling of the pure oxygen column is achieved by a fraction of the flow of gaseous air leaving the main exchange line, compressed by a booster at the pressure required for the vaporization of oxygen in the vaporizer (HP air). This fraction of air HP condenses partially or totally in the condenser of the pure oxygen column.
Selon une variante, le débit d'air surpressé partiellement condensé, éventuellement après avoir séparé la partie condensée (qui est alors envoyée dans la colonne MP), est ensuite envoyé dans le vaporiseur produit où il finit de se condenser totalement. La condensation partielle de l'air surpressé permet, avec un débit quasi-nominal de production du GOX et la même pression, de faire fonctionner le vaporiseur en cuve de colonne pur, puis celui du vaporiseur produit. Le rebouillage de la colonne d'oxygène liquide pur est donc gratuit par rapport à l'énergie nécessaire pour vaporiser la production.  According to a variant, the partially condensed compressed air flow, possibly after having separated the condensed part (which is then sent into the MP column), is then sent into the product vaporizer where it finishes to condense completely. The partial condensation of the supercharged air allows, with a quasi-nominal flow of GOX production and the same pressure, to operate the vaporizer in pure column vat, then that of the vaporizer produced. The reboiling of the pure liquid oxygen column is therefore free compared to the energy required to vaporize the production.
La pression de ce débit d'air est supérieure à la pression de la colonne MP (typiquement de l'ordre de 4,5 bar abs. contre 3,2 bar abs.).  The pressure of this air flow is greater than the pressure of the MP column (typically of the order of 4.5 bar abs against 3.2 bar abs.).
On prélève une partie du liquide impur dans le vaporiseur produit (au même niveau et à la place de la purge de déconcentration du vaporiseur) que l'on envoie dans la colonne d'oxygène l iquide pur qui est une colonne à distiller sensiblement à la même pression que le vaporiseur produit..  Part of the impure liquid is removed from the vaporizer produced (at the same level and instead of the purge of the evaporator), and the pure liquid is sent to the column of oxygen which is a distillation column which is substantially distilled off. same pressure as the vaporizer produces ..
Le reflux gazeux impur issu de la colonne d'oxygène pur est mélangé avec le flux gazeux issu du vaporiseur produit, les deux flux constituant le débit nominal de production du GOX impur.  The impure gas reflux from the pure oxygen column is mixed with the gas stream from the product vaporizer, the two flows constituting the nominal output flow of the impure GOX.
Le liquide pur est prélevé en cuve de la colonne d'oxygène pur. Il sert aussi de purge de déconcentration de l'ensemble de l'appareil.  The pure liquid is taken from the vat of the pure oxygen column. It also serves as a purge of deconcentration of the entire device.
L'appoint de frigories peut être apporté par un liquéfacteur indépendant, par exemple par production d'azote liquide, à partir d'azote pur (issu d'un minaret), qui serait alors rajouté sous forme liquide dans l'appareil. S'il n'y a pas de production d'azote pur l iqu ide, on peut envisager de liquéfier de l'azote résiduaire dans un liquéfacteur indépendant.  The addition of frigories can be provided by an independent liquefier, for example by producing liquid nitrogen, from pure nitrogen (from a minaret), which would then be added in liquid form in the apparatus. If there is no pure nitrogen production, it is possible to liquefy residual nitrogen in an independent liquefier.
Si la production de liquide pur est faible, on peut aussi envisager d'avoir un système de production de froid intégré à l'ASU.  If the production of pure liquid is low, one can also consider having a system of cold production integrated into the ASU.
L'invention sera décrite en plus de détail en se référant aux figures, qui illustrent des procédés de séparation d'air selon l'invention. Dans la Figure 1 , l'air est séparé dans un ASU comprenant une double colonne de séparation d'air, comprenant une colonne moyenne pression 23 et une colonne basse pression 25. Des frigories pour la séparation sont fournies par détente d'azote moyenne pression dans une turbine 47. L'appareil comprend une colonne d'oxygène liquide pur 49, une pompe 57, un vaporiseur 51 et une ligne d'échange 63. The invention will be described in more detail with reference to the figures, which illustrate air separation methods according to the invention. In FIG. 1, the air is separated in an ASU comprising a double air separation column, comprising a medium pressure column 23 and a low pressure column 25. Frigories for the separation are provided by expansion of medium pressure nitrogen. in a turbine 47. The apparatus comprises a column of pure liquid oxygen 49, a pump 57, a vaporizer 51 and an exchange line 63.
L'air 1 est pressurisé par un compresseur 3 à une pression entre 2,5 et 4,5 bars abs. L'air est ensuite épuré dans une unité d'épuration 5 par adsoprtion. L'air épu ré 7 est d ivisé en deux parties . U ne partie 9 est surpressée dans un surpresseur 13 jusqu'à une pression d'entre 4. et 20 bars abs et puis refroidie dans la ligne d'échange 63 jusqu'au bout froid. L'air 9 est divisé en deux fractions 15, 17. Une fraction 1 5 est envoyée au vaporiseur 51 où elle sert à vaporiser partiellement de l'oxygène liquide comprenant au plus 97 % mol. d'oxygène, pour produire l'oxygène gazeux 59 qui se réchauffe dans la ligne d'échange 63. Ce gaz 59 est envoyé à une unité d'oxycombustion. Un liquide riche en oxygène 53 est soutiré du vaporiseur 51 comme purge. L'air se trouve condensé. L'autre fraction de l'air 17 est envoyée au rebouilleur de cuve 61 de la colonne d'oxygène pur 49. Cette colonne comporte le rebouilleur de cuve et des moyens d'échange de chaleur et de matière au-dessus de ce rebouilleur. De l'oxygène liquide 65 comprenant au plus 97% mol. d'oxygène est envoyé en tête de la colonne 49 et s'enrichit pour former le produit liquide 71 soutiré en cuve et contenant au moins 98% mol. d'oxygène. L'oxygène gazeux de tête de la colonne 49 est envoyé en cuve de la colonne basse pression 25. L'air condensé 17 se mélange avec l'air condensé provenant du vaporiseur 51 et, après détente dans une vanne 21 , est envoyé à la colonne MP 23, qui opère à entre 2,5 et 4,5 bars abs.  Air 1 is pressurized by a compressor 3 at a pressure between 2.5 and 4.5 bar abs. The air is then purified in a purification unit 5 by adsorption. The air fresh 7 is divided into two parts. Part 9 is overpressed in a booster 13 to a pressure of between 4 and 20 bar abs and then cooled in the exchange line 63 to the cold end. The air 9 is divided into two fractions 15, 17. A fraction 1 5 is sent to the vaporizer 51 where it serves to partially vaporize liquid oxygen comprising at most 97 mol%. oxygen, to produce gaseous oxygen 59 which is heated in the exchange line 63. This gas 59 is sent to an oxyfuel unit. An oxygen-rich liquid 53 is withdrawn from the vaporizer 51 as a purge. The air is condensed. The other fraction of the air 17 is sent to the reboiler 61 of the pure oxygen column 49. This column comprises the reboiler vessel and means for exchanging heat and material above the reboiler. Liquid oxygen 65 comprising at most 97 mol%. oxygen is sent to the top of the column 49 and is enriched to form the liquid product 71 withdrawn into the tank and containing at least 98 mol%. oxygen. The gaseous oxygen at the top of the column 49 is sent to the bottom of the low pressure column 25. The condensed air 17 mixes with the condensed air coming from the vaporizer 51 and, after expansion in a valve 21, is sent to the MP 23 column, which operates at between 2.5 and 4.5 bar abs.
Une autre partie 1 1 de l'air est refroidie dans la ligne d'échange 63, est envoyée au rebouilleur de cuve 35 de la colonne BP 25, s'y condense au moins partiellement et est envoyée en cuve de la colonne MP 23, en dessous du point d'arrivée d'air liquide 19.  Another part 1 1 of the air is cooled in the exchange line 63, is sent to the bottom reboiler 35 of the column BP 25, condenses at least partially and is sent to the bottom of the column MP 23, below the point of arrival of liquid air 19.
Du liquide enrichi en oxygène 27 est soutiré de la cuve de la colonne MP Oxygen-enriched liquid 27 is withdrawn from the tank of the MP column
23, refroidi dans le sous-refroidisseur 33, détendu et envoyé à la colonne BP 25. Du liquide 29 est soutiré de la colonne MP 23, refroidi dans le sous-refroidisseur 33, détendu et envoyé à la colonne BP 25. Du liquide riche en azote 31 est soutiré de la tête de la colonne MP 23, refroidi dans le sous-refroidisseur 33, détendu et envoyé à la tête de la colonne BP 25. 23, cooled in the subcooler 33, expanded and sent to the LP column 25. Liquid 29 is withdrawn from the MP column 23, cooled in the subcooler 33, expanded and sent to the BP column 25. Rich liquid in nitrogen 31 is withdrawn from the head of the MP column 23, cooled in the subcooler 33, expanded and sent to the head of the BP column 25.
De l'azote basse pression 39 est soutiré en tête de la colonne BP, réchauffé dans le sous-refroidisseur 33 et réchauffé dans la ligne d'échange 63.  Low pressure nitrogen 39 is withdrawn at the top of the LP column, reheated in the subcooler 33 and reheated in the exchange line 63.
De l'azote moyenne pression 41 est divisé en deux pour former une partie Medium pressure nitrogen 41 is divided in two to form a part
43 et une partie 45. La partie 43 sert à chauffer le rebouilleur intermédiaire 37 de la colonne basse pression 25. La partie 45 se réchauffe dans la ligne d'échange 63, est détendue dans la turbine 47 et est renvoyée à la ligne d'échange 63. De l'oxygène liquide est soutiré de la cuve de la colonne BP et divisé en deux. Une partie 55 est pressurisée dans la pompe 57 en amont du vaporiseur 51 et le reste 65 est envoyé en tête de la colonne d'oxygène pur 49 sans avoir été pressurisé. La tête de la colonne d'oxygène pur 49 se trouve donc à la même pression que la cuve de la colonne basse pression 25. Tout ou une partie du liquide de purge 53 peut également alimenter la tête de la colonne 49. 43 and a portion 45. The portion 43 serves to heat the intermediate reboiler 37 of the low pressure column 25. The portion 45 is heated in the exchange line 63, is expanded in the turbine 47 and is returned to the line of exchange 63. Liquid oxygen is withdrawn from the tank of the LP column and divided in two. A portion 55 is pressurized in the pump 57 upstream of the vaporizer 51 and the remainder 65 is sent to the top of the pure oxygen column 49 without having been pressurized. The head of the pure oxygen column 49 is therefore at the same pressure as the tank of the low pressure column 25. All or part of the purge liquid 53 can also feed the head of the column 49.
Un débit de liquide cryogénique 69, par exemple de l'azote liquide, est envoyé en tête de la colonne BP pour tenir le procédé en froid.  A flow of cryogenic liquid 69, for example liquid nitrogen, is sent to the top of the LP column to keep the process cold.
Le procédé de la Figure 1 bis diffère de celui de la Figure 1 en ce que la colonne 49 est alimentée en tête exclusivement par la purge 53 du vaporiseur 51 , suite à une étape de détente dans une vanne. Le rebouilleur de cuve 61 de la colonne 49 est toujours chauffé par l'air surpressé 17, l'air ainsi condensé étant mélangé avec l'air surpressé 15 qui a servi à chauffer le vaporiseur 51 . Il est également possible d'alimenter la colonne avec du liquide de purge 53 et de l'oxygène liquide 65 provenant de la cuve de la colonne basse pression 25.  The method of FIG. 1 bis differs from that of FIG. 1 in that the column 49 is fed exclusively at the top by the purge 53 of the vaporizer 51, following a step of expansion in a valve. The reboiler 61 of the column 49 is still heated by the pressurized air 17, the air thus condensed being mixed with the pressurized air 15 which was used to heat the vaporizer 51. It is also possible to feed the column with purge liquid 53 and liquid oxygen 65 from the bottom of the low pressure column 25.
Le procédé de la Figure 2 diffère de celui de la Figure 1 en ce que le débit d'air 9 est envoyé d'abord au vaporiseur de cuve 61 de la colonne d'oxygène pur 49 et ensuite au vaporiseur 51 où il se condense. L'air ainsi formé est détendu dans la vanne 21 et envoyé à la colonne moyenne pression 23. La fraction d'air 1 1 se refroidit dans la ligne d'échange 1 1 et est envoyée à la cuve de la colonne moyenne pression 23 sans avoir été détendue ou comprimée en aval du compresseur 3.  The method of Figure 2 differs from that of Figure 1 in that the air flow 9 is first sent to the vessel vaporizer 61 of the pure oxygen column 49 and then to the vaporizer 51 where it condenses. The air thus formed is expanded in the valve 21 and sent to the medium pressure column 23. The air fraction 1 1 cools in the exchange line January 1 and is sent to the tank of the medium pressure column 23 without have been relaxed or compressed downstream of the compressor 3.
Le rebouilleur intermédiaire 37 est toujours chauffé par de l'azote moyenne pression 43 mais une autre partie de l'azote moyenne pression 73 est comprimée dans un surpresseur froid 71 à partir d'une température cryogénique et envoyée au rebouilleur de cuve 35. L'azote condensé est détendu dans une vanne 36 et envoyé en tête de la colonne MP 23. L'oxygène de cuve 55 de la colonne basse pression est entièrement pressurisé dans la pompe 57 envoyé au vaporiseur 51 où il se vaporise partiellement. Le gaz vaporisé constitue le produit d'oxygène gazeux 59 contenant moins que 97% mol. d'oxygène. Le liquide non-vaporisé 53 alimente la tête de la colonne 49. L'oxygène gazeux 67 de tête de la colonne 49 est mélangé avec l'oxygène gazeux 59. L'oxygène liquide 71 constitue le produit liquide. Dans ce cas, la colonne d'oxygène pur 49 n'opère pas à la même pression que la colonne BP 25. Intermediate reboiler 37 is still heated by medium pressure nitrogen 43 but another part of medium pressure nitrogen 73 is compressed in a cold booster 71 from a cryogenic temperature and sent The condensed nitrogen is expanded in a valve 36 and sent to the top of the MP column 23. The vessel oxygen 55 of the low pressure column is fully pressurized in the pump 57 sent to the vaporizer 51 where it partially vaporizes. The vaporized gas is the gaseous oxygen product 59 containing less than 97 mol%. oxygen. The non-vaporized liquid 53 feeds the top of the column 49. The gaseous oxygen 67 at the top of the column 49 is mixed with the oxygen gas 59. The liquid oxygen 71 constitutes the liquid product. In this case, the pure oxygen column 49 does not operate at the same pressure as the BP column 25.
Le procédé de la Figure 1 ou 1 bis peut utiliser de l'azote pour chauffer le rebouilleur de cuve 35 et le procédé de la Figure 2 peut utiliser de l'air pour chauffer le rebouilleur de cuve 35.  The process of Figure 1 or 1a may use nitrogen to heat the bottom reboiler 35 and the method of Figure 2 may use air to heat the bottom reboiler 35.

Claims

Revendications claims
1 . Procédé de séparation d'air par distillation cryogénique dans une unité de séparation comprenant une colonne moyenne pression (23) et une colonne basse pression (25), reliées thermiquement entre elles, la colonne basse pression comprenant un rebouilleur de cuve (35) et un rebouilleur intermédiaire (37) et une colonne d'oxygène pur (49) dans lequel 1. A method of separating air by cryogenic distillation in a separation unit comprising a medium pressure column (23) and a low pressure column (25), thermally connected to each other, the low pressure column comprising a bottom reboiler (35) and a intermediate reboiler (37) and a pure oxygen column (49) in which
i) on envoie de l'air gazeux épuré puis refroidi à une première pression dans une ligne d'échange à la colonne moyenne pression,  i) purified air gas is sent and then cooled to a first pressure in an exchange line at the medium pressure column,
ii) on envoie un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression,  ii) an oxygen-enriched liquid and a nitrogen-enriched liquid are sent from the medium-pressure column to the low-pressure column,
iii) on soutire un gaz riche en azote de la colonne basse pression, iv)on soutire un liquide riche en oxygène contenant au plus 97% mol. d'oxygène en cuve de la colonne basse pression,  iii) a nitrogen rich gas is withdrawn from the low pressure column, iv) an oxygen-rich liquid containing at most 97 mol% is withdrawn. of oxygen in the tank of the low pressure column,
v) on envoie un premier débit de liquide riche en oxygène à un vaporiseur (51 ) et on envoie l'oxygène gazeux ainsi formé à la ligne d'échange,  v) a first flow of oxygen-rich liquid is sent to a vaporizer (51) and the gaseous oxygen thus formed is sent to the exchange line,
vi) on envoie un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur, ayant un rebouilleur de cuve (61 ), où il s'épure pour former un liquide de cuve contenant au moins 98% mol. d'oxygène,  vi) a second flow of oxygen-rich liquid is fed to the top of the pure oxygen column, having a bottom reboiler (61), where it purifies to form a bottom liquid containing at least 98 mol%. oxygen,
vii) on envoie un débit d'air surpressé à une deuxième pression, supérieure à la première pression, au rebouilleur de cuve de la colonne d'oxygène pur,  vii) a superpressed air flow is sent at a second pressure, higher than the first pressure, to the vessel reboiler of the pure oxygen column,
viii) on soutire un gaz riche en azote en tête de la colonne moyenne pression, on l'envoie au rebouilleur intermédiaire de la colonne basse pression et on envoie le gaz condensé à la tête de la colonne moyenne pression, et  viii) a nitrogen rich gas is withdrawn at the top of the medium pressure column, it is sent to the intermediate reboiler of the low pressure column and the condensed gas is sent to the head of the medium pressure column, and
ix) on envoie un gaz riche en azote ou de l'air au rebouilleur de cuve de la colonne basse pression et on envoie le liquide qui s'y condense à la colonne moyenne pression  ix) a nitrogen-rich gas or air is sent to the bottom reboiler of the low pressure column and the liquid which is condensed therein is sent to the medium pressure column
caractérisé en ce que l'on soutire du liquide de cuve de la colonne d'oxygène pur comme produit et en ce que l'on envoie de l'air surpressé à la deuxième pression au vaporiseur pour vaporiser le premier débit de liquide riche en oxygène. characterized in that vessel liquid is withdrawn from the pure oxygen column as product and superpressed air is supplied to the second vaporizer pressure to vaporize the first oxygen-rich liquid flow. .
2. Procédé selon la revendication 1 dans lequel on pressurise le premier débit de liquide riche en oxygène en amont du vaporiseur (51 ). 2. Method according to claim 1 wherein the first oxygen-rich liquid flow is pressurized upstream of the vaporizer (51).
3. Procédé selon la revendication 1 ou 2 dans lequel le premier débit de liquide riche en oxygène et le deuxième débit de liquide riche en oxygène ont la même pureté. 3. The method of claim 1 or 2 wherein the first flow of oxygen-rich liquid and the second flow of oxygen-rich liquid have the same purity.
4. Procédé selon la revendication 3 dans lequel on divise de l'air surpressé à la deuxième pression en deux parties, on envoie une première partie d'air surpressé à la deuxième pression au rebouilleur de cuve de la colonne d'oxygène pur et on envoie une deuxième partie d'air surpressé à la deuxième pression au vaporiseur (51 ). 4. The method of claim 3 wherein the supercharged air is divided at the second pressure into two parts, a first portion of superpressed air is sent to the second tank reboiler pressure of the pure oxygen column and sends a second portion of supercharged air at the second pressure to the vaporizer (51).
5. Procédé selon la revendication 1 ou 2 dans lequel le premier débit de liquide riche en oxygène est moins riche en oxygène que le deuxième débit de liquide riche en oxygène. The method of claim 1 or 2 wherein the first flow of oxygen-rich liquid is less oxygen-rich than the second oxygen-rich flow of oxygen.
6. Procédé selon la revendication 5 dans lequel le premier débit de liquide riche en oxygène se vaporise partiellement dans le vaporiseur (51 ), le liquide formé constituant le deuxième débit de liquide riche en oxygène. 6. The method of claim 5 wherein the first flow of oxygen-rich liquid partially vaporizes in the vaporizer (51), the formed liquid constituting the second flow of oxygen-rich liquid.
7. Procédé selon la revendication 6 dans lequel le débit d'air surpressé à la deuxième pression chauffe d'abord le rebouilleur de cuve (61 ) de la colonne d'oxygène pur (49) et ensuite le vaporiseur (51 ). 7. The method of claim 6 wherein the compressed air flow rate at the second pressure first heats the bottom reboiler (61) of the pure oxygen column (49) and then the vaporizer (51).
8. Procédé selon l'une des revendications précédentes dans lequel un liquide cryogénique (69) d'une source auxiliaire est envoyé à la double colonne. 8. Method according to one of the preceding claims wherein a cryogenic liquid (69) of an auxiliary source is sent to the double column.
9. Appareil de séparation d'air par distillation cryogénique comprenant une colonne moyenne pression (23) et une colonne basse pression (25), reliées thermiquement entre elles, la colonne basse pression comprenant un rebouilleur de cuve (35) et un rebouilleur intermédiaire (37) et une colonne d'oxygène pur (49), une ligne d'échange (63), un vaporiseur (51 ), des moyens pour envoyer de l'air gazeux épuré puis refroidi à une première pression de la ligne d'échange à la colonne moyenne pression, des moyens pour envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, des moyens pour soutirer un gaz riche en azote de la colonne basse pression, des moyens pour soutirer un liquide riche en oxygène contenant au plus 97% mol. d'oxygène en cuve de la colonne basse pression, des moyens pour envoyer un premier débit de liquide riche en oxygène au vaporiseur, une conduite pour envoyer l'oxygène gazeux ainsi formé à la ligne d'échange, des moyens pour envoyer un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur, ayant un rebouilleur de cuve (61 ), où il s'épure pour former un liquide de cuve contenant au moins 98% mol. d'oxygène, un surpresseur (3), une conduite pour envoyer un débit d'air surpressé (17) à une deuxième pression supérieure à la première pression au rebouilleur de cuve de la colonne d'oxygène pur, des conduites pour soutirer un gaz riche en azote en tête de la colonne moyenne pression, pour l'envoyer au rebouilleur intermédiaire de la colonne basse pression et pour envoyer le gaz condensé à la tête de la colonne moyenne pression et des conduites pour envoyer un gaz riche en azote ou de l'air au rebouilleur de cuve de la colonne basse pression et pour envoyer le liquide qui s'y condense à la colonne moyenne pression caractérisé en ce qu'il comprend une conduite pour soutirer du liquide de cuve (71 ) de la colonne d'oxygène pur comme produit et des moyens pour envoyer de l'air surpressé (15) à la deuxième pression du surpresseur au vaporiseur. 9. Apparatus for separating air by cryogenic distillation comprising a medium pressure column (23) and a low pressure column (25), thermally connected to each other, the low pressure column comprising a bottom reboiler (35) and an intermediate reboiler ( 37) and a column of pure oxygen (49), an exchange line (63), a vaporizer (51), means for sending purified air gas and then cooled at a first pressure of the exchange line to the medium pressure column, means for supplying an oxygen enriched liquid and a nitrogen enriched liquid from the medium pressure column to the low pressure column, means for withdrawing a nitrogen rich gas from the low pressure column, means for withdrawing an oxygen rich liquid containing at most 97 mol% of oxygen in the tank of the low pressure column, means for sending a first flow of oxygen-rich liquid to the vaporizer, a pipe for sending the gaseous oxygen thus formed to the exchange line, means for sending a second flow oxygen-rich liquid at the top of the pure oxygen column, having a bottom reboiler (61), where it purifies to form a bottom liquid containing at least 98 mol%. an oxygen booster, a booster (3), a conduit for supplying a pressurized air flow (17) at a second pressure higher than the first tank reboiler pressure of the pure oxygen column, lines for withdrawing a gas nitrogen rich at the top of the medium pressure column, to send it to the intermediate reboiler of the low pressure column and to send the condensed gas to the head of the medium pressure column and lines to send a gas rich in nitrogen or air to the bottom reboiler of the low pressure column and to send the liquid which condenses therein to the medium pressure column characterized in that it comprises a pipe for withdrawing the tank liquid (71) from the oxygen column pure product and means for supplying pressurized air (15) at the second pressure of the booster to the vaporizer.
10. Appareil selon la revendication 9 comprenant : Apparatus according to claim 9 comprising:
i) une conduite pour envoyer un liquide (53) du vaporiseur (51 ) en tête de la colonne d'oxygène pur (49) et/ou  i) a pipe for sending a liquid (53) of the vaporizer (51) at the top of the pure oxygen column (49) and / or
ii) une conduite pour envoyer un liquide de cuve (65) de la colonne basse pression (25) en tête de la colonne d'oxygène pur (49).  ii) a line for sending a bottom liquid (65) from the low pressure column (25) to the top of the pure oxygen column (49).
1 1 . Appareil selon la revendication 10 dans les moyens pour envoyer l'air surpressé du surpresseur (3) au vaporiseur (51 ) sont reliés au rebouilleur de cuve (61 ) de la colonne d'oxygène pur (49) de sorte que l'air destiné au vaporiseur passe à travers le rebouilleur de cuve de la colonne d'oxygène pur. 1 1. Apparatus according to claim 10 in the means for sending the supercharged air of the booster (3) to the vaporizer (51) are connected to the reboiler (61) of the pure oxygen column (49) so that air for the vaporizer passes through the bottom reboiler of the pure oxygen column.
12. Appareil selon la revendication 9 ou 1 0 dans lequel les moyens pour envoyer un deuxième débit de liquide riche en oxygène en tête de la colonne d'oxygène pur sont constitués par la conduite pour envoyer un liquide de cuve de la colonne basse pression (65) en tête de la colonne d'oxygène pur (49). Apparatus according to claim 9 or 10 wherein the means for sending a second flow of oxygen-rich liquid to the top of the pure oxygen column is constituted by the conduit for supplying a bottom liquid from the low pressure column ( 65) at the top of the pure oxygen column (49).
13. Appareil selon la revendication 9,10 ou 12 comprenant des moyens pour diviser l'air surpressé à la deuxième pression en deux parties, les moyens pour envoyer de l'air surpressé à la deuxième pression du surpresseur (3) au vaporiseur (51 ) et la conduite pour envoyer un débit d'air surpressé à la deuxième pression au rebouilleur de cuve (61 ) de la colonne d'oxygène pur (49) étant reliés de sorte qu'une partie d'air surpressé (17) est envoyée au rebouilleur de cuve de la colonne d'oxygène pur et une autre partie d'air surpressé (15) est envoyée au vaporiseur. Apparatus according to claim 9, 10 or 12 including means for dividing the supercharged air at the second pressure into two parts, the means for supplying superpressed air at the second pressure of the booster (3) to the vaporizer (51). ) and the pipe for sending an overpressurized air flow to the second tank reboiler pressure (61) of the pure oxygen column (49) being connected so that a portion of pressurized air (17) is sent at the vessel reboiler of the pure oxygen column and another portion of pressurized air (15) is sent to the vaporizer.
14. Appareil selon l'une des revendications 9 à 13 comprenant une conduite pour envoyer un liquide (53) du vaporiseur (51 ) en tête de la colonne d'oxygène pur (49) et une conduite pour envoyer un liquide de cuve (65) de la colonne basse pression (25) en tête de la colonne d'oxygène pur (49). 14. Apparatus according to one of claims 9 to 13 comprising a pipe for sending a liquid (53) of the vaporizer (51) at the top of the pure oxygen column (49) and a pipe for sending a liquid tank (65). ) of the low pressure column (25) at the top of the pure oxygen column (49).
15. Appareil selon l'une des revendications 9 à 14 comprenant des moyens (69) pour envoyer un liquide cryogénique à la colonne basse pression d'une source extérieure. 15. Apparatus according to one of claims 9 to 14 comprising means (69) for sending a cryogenic liquid to the low pressure column of an external source.
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FR2973865A1 (en) 2012-10-12
FR2973865B1 (en) 2015-11-06
AU2012238460A1 (en) 2013-10-31
CA2830826C (en) 2018-10-16
CN103842753B (en) 2016-12-07
EP2694898B1 (en) 2020-06-17
US20140053601A1 (en) 2014-02-27
WO2012136939A3 (en) 2015-01-22
CN103842753A (en) 2014-06-04
WO2012136939A2 (en) 2012-10-11
AU2012238460B2 (en) 2016-12-22
US9696087B2 (en) 2017-07-04
CA2830826A1 (en) 2012-10-11

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