EP2686628B1 - Appareil et procede de separation d'air par distillation cryogenique - Google Patents

Appareil et procede de separation d'air par distillation cryogenique Download PDF

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Publication number
EP2686628B1
EP2686628B1 EP12714763.5A EP12714763A EP2686628B1 EP 2686628 B1 EP2686628 B1 EP 2686628B1 EP 12714763 A EP12714763 A EP 12714763A EP 2686628 B1 EP2686628 B1 EP 2686628B1
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EP
European Patent Office
Prior art keywords
oxygen
exchanger
pressure
air
purge
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EP12714763.5A
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German (de)
English (en)
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EP2686628A2 (fr
Inventor
Marie Cognard
Benoit Davidian
Richard Dubettier-Grenier
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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
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Publication of EP2686628A2 publication Critical patent/EP2686628A2/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—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
    • F25J3/0228—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 characterised by the separated product stream
    • 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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • 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
    • F25J2200/50—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
    • 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
    • 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
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the present invention relates to an apparatus and method for separating air by air distillation, according to the preambles of claims 1 and 3 respectively and known from document WO-A-10/109149 .
  • the oxygen gas can optionally contain less than 98 mol%. oxygen.
  • He is known to WO-A-10/109149 to vaporize a flow of liquid oxygen at low pressure in an external vaporizer to produce gaseous oxygen which is then heated in a main exchanger.
  • the present invention proposes to vaporize the deconcentration purge of a vaporizer in an exchanger in order to recover the frigories, this vaporizer being the exchanger making it possible to vaporize a liquid from the device under pressure to produce a gaseous product under pressure.
  • the apparatus comprises an exchange line 21 and a double column consisting of a medium pressure column 27 and a low pressure column 29.
  • All the air 1 is compressed in the main compressor 2 to produce air at the pressure P1 substantially equal to the pressure of the medium pressure column 27.
  • the air at the pressure P1 is cooled in a cooler 7, purified in a purification unit 9 and divided into three fractions.
  • the first fraction 11 is boosted in a booster, which may be formed by the last stage of the main compressor, the last stage which is part of the second part of the compressor.
  • the pressure P1 is less than 5 bars abs, even at 4.5 bar abs, preferably less than 4 bar, and even less than 3.5 bar abs
  • the first fraction 11 is brought to a pressure P2 by the booster 5 or an independent compressor 5 and cools to this pressure in a cooler (not shown) before being sent to the exchange line 21.
  • the line of exchange consists of an indirect heat exchanger in aluminum with brazed plates.
  • Fraction 11 is then sent in gaseous form to a vaporizer 41 where it condenses at least partially before being expanded and sent to the medium pressure column 27.
  • the pressure P2 is less than 15 bar abs, preferably less than 10 bar, and still less than 6 bar abs.
  • Fraction 11 is less than half of flow 1, and preferably less than one third of flow 1
  • the second fraction 13 at pressure P1 cools completely in the exchange line 21 and is divided into two flows.
  • the first stream 23 is sent to a bottom reboiler 33 of the low pressure column 29 where it condenses at least partially and is sent to the medium pressure column, mixed with the flow 11.
  • the second stream 25 is sent in gaseous form to the medium pressure column 27.
  • the third fraction 15 is boosted in a booster 17, partially cooled in the exchange line 21, withdrawn from the exchange line at an intermediate level thereof and expanded in a turbine 19 coupled to the booster 17 before being sent to the low pressure column 29.
  • a liquid flow enriched in oxygen 55, an intermediate flow 53 and a liquid flow rich in nitrogen 51 are withdrawn from the medium pressure column 27, cooled in the exchanger 31, expanded and sent to different levels of the low pressure column 29 .
  • Medium pressure gaseous nitrogen 49 is condensed in an intermediate vaporizer 35 of low pressure column 29 and sent as reflux to the top of medium pressure column 27.
  • Another medium pressure gaseous nitrogen flow 47 is heated in line d 'exchange.
  • Liquid oxygen 37 containing at least 80 mol%. oxygen and optionally at most 98 mol%. of oxygen, is withdrawn from the bottom of the low pressure column 29, pressurized by a pump 39 to a pressure less than 9 bars abs, or even less than 5 bars abs and sent to the vaporizer 41. Apart from a purge of liquid 43, the oxygen vaporizes in the vaporizer 41 by heat exchange with the air fraction 11 at the pressure P2. This oxygen then forms the first pressurized gaseous oxygen flow 45 which heats up in the exchange line 21. The air fraction 11 is partially condensed and is sent to the double column.
  • the purge liquid 43 is pressurized to a pressure of at least 10 bar abs, or at least 15 bar abs, or even at least 20 bar abs in a pump 63 and then vaporizes in the exchange line 21.
  • the second gas flow thus produced 59 is sent to a pressurized gas storage 3 and expanded to be mixed with the flow 45 via line 61.
  • the vaporization of the purge liquid is carried out using mainly sensible heat, so that no air flow leaving the exchanger 21 is totally condensed, or even condensed.
  • the pressurized purge liquid 43 can be vaporized in an auxiliary exchanger 21A, separate from the exchange line, against an air flow 25A and with a flow of refrigerant, for example a flow of nitrogen 57A heating up from the separation process.
  • the flow 25A cooled in the exchanger 21A mixes with the cooled flow 25 and the nitrogen flow 57A heated in the exchanger 21A mixes with the heated flow 57.
  • the second flow of gaseous oxygen 59, 61 formed by the vaporization can be used as a back-up gas when the production of gaseous oxygen 45 is interrupted.
  • a varying amount of the second oxygen gas flow rate is mixed with the first flow rate to produce a substantially constant mixed flow rate.
  • This variable quantity of the vaporized purge liquid can be mixed with the first flow rate 45 to smooth out the variations in flow rates, due, for example, to variations in the pressure of the oxygen network.
  • oxygen By sensing a reduction in pressure in line 45, due, for example, to increased demand for oxygen, oxygen can be expanded and sent from storage 3 to line 45 through line 61.
  • the oxygen flow 45 will reduce or be nonexistent.
  • the oxygen flow 63 of the storage 3 can supply a customer, the time that an emergency vaporizer starts up to avoid any production stoppage.
  • Flow 37 is the only flow containing more than 60 mol%. of oxygen withdrawn from the low pressure column.
  • Storage 3 operates at a higher pressure than flow 45.

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

Description

  • La présente invention est relative à un appareil et procédé de séparation d'air par distillation d'air, conformément aux préambules des revendications 1 et 3 respectivement et connu du document WO-A-10/109149 .
  • En particulier elle concerne la production d'oxygène gazeux à une pression inférieure à 9 bars abs, voire inférieure à 5 bars abs. L'oxygène gazeux peut éventuellement contenir moins de 98% mol. d'oxygène.
  • Il est nécessaire de produire de grandes quantités d'oxygène ayant ces caractéristiques pour alimenter les appareils d'oxycombustion, entre autres.
  • Il est connu de WO-A-10/109149 de vaporiser un débit d'oxygène liquide à basse pression dans un vaporiseur extérieur pour produire de l'oxygène gazeux qui se réchauffe ensuite dans un échangeur principal.
  • Il est connu de vaporiser la purge d'une colonne de distillation afin d'en récupérer les frigories, par exemple dans US-A-5408831 .
  • US-A-5765396 et US-A-5251451 décrivent des installations selon le préambule de la revendication 1.
  • Par contre la présente invention propose de vaporiser la purge de déconcentration d'un vaporiseur dans un échangeur afin de récupérer les frigories, ce vaporiseur étant l'échangeur permettant de vaporiser un liquide de l'appareil sous pression pour produire un produit gazeux sous pression.
  • Il est souhaitable d'envoyer la purge à un stockage gazeux sous pression permettant de maintenir une production stable aussi bien en débit, qu'en pression.
  • Selon un objet de l'invention, il est prévu un appareil selon la revendication 1.
  • Optionnellement :
    • l'échangeur relié à la conduite d'oxygène de purge est l'échangeur principal.
    • l'échangeur relié à la conduite d'oxygène de purge est un échangeur distinct de l'échangeur principal.
    • l'échangeur comprend des passages reliés à une conduite d'amenée d'air d'alimentation et des passages reliés à une conduite d'amenée de fluide frigorigène, provenant éventuellement de la double colonne.
  • Selon un autre objet de l'invention, il est prévu un procédé selon la revendication 3.
  • Optionnellement :
    • l'oxygène de purge est pressurisé à une pression d'au moins 10 bars abs, de préférence au moins 15 bars abs, voire au moins 20 bars abs dans la deuxième pompe.
    • l'oxygène de purge se vaporise dans l'échangeur principal.
    • l'oxygène de purge se vaporise dans un échangeur autre que l'échangeur principal.
    • une quantité variable du deuxième débit d'oxygène gazeux est mélangée avec le premier débit afin de produire un débit mélangé substantiellement constant.
    • l'oxygène liquide soutiré de la colonne basse pression contient au moins 80% mol. d'oxygène
    • l'oxygène liquide soutiré de la colonne basse pression constitue le seul débit contenant au moins 80% mol. d'oxygène soutiré de la colonne basse pression.
    • l'oxygène liquide soutiré de la colonne basse pression contient au plus 98% mol. d'oxygène.
  • L'invention sera décrite en plus de détail en se référant aux figures qui illustrent des appareils de séparation d'air selon l'invention.
  • Dans la Figure 1, l'appareil comprend une ligne d'échange 21 et une double colonne constituée par une colonne moyenne pression 27 et une colonne basse pression 29.
  • Tout l'air 1 est comprimé dans le compresseur principal 2 pour produire de l'air à la pression P1 substantiellement égale à la pression de la colonne moyenne pression 27. L'air à la pression P1 est refroidi dans un refroidisseur 7, épuré dans une unité d'épuration 9 et divisé en trois fractions. La première fraction 11 est surpressée dans un surpresseur, pouvant être constitué par le dernier étage du compresseur principal, dernier étage qui fait partie de la deuxième partie du compresseur. La pression P1 est inférieure à 5 bars abs, voire à 4.5 bar abs, préférablement inférieure à 4 bar, et encore inférieure à 3.5 bar abs
  • La première fraction 11 est amenée à une pression P2 par le booster 5 ou un compresseur indépendant 5 et se refroidit à cette pression dans un refroidisseur (non-illustré) avant d'être envoyé à la ligne d'échange 21. La ligne d'échange est constituée par un échangeur de chaleur indirect en aluminium à plaques brasées. La fraction 11 est ensuite envoyée sous forme gazeuse à un vaporiseur 41 où elle se condense au moins partiellement avant d'être détendue et envoyée à la colonne moyenne pression 27. La pression P2 est inférieure à 15 bar abs, préférablement inférieure à 10 bar, et encore inférieure à 6 bar abs. La fraction 11 est inférieure à la moitié du débit 1, et préférentiellement inférieure à un tiers du débit 1
  • La deuxième fraction 13 à la pression P1 se refroidit complètement dans la ligne d'échange 21 et est divisée en deux flux. Le premier flux 23 est envoyé à un rebouilleur de cuve 33 de la colonne basse pression 29 où il se condense au moins partiellement et est envoyé à la colonne moyenne pression, mélangé au débit 11. Le deuxième flux 25 est envoyé sous forme gazeuse à la colonne moyenne pression 27.
  • La troisième fraction 15 est surpressée dans un surpresseur 17, refroidie partiellement dans la ligne d'échange 21, soutirée de la ligne d'échange à un niveau intermédiaire de celle-ci et détendue dans une turbine 19 couplée au surpresseur 17 avant d'être envoyée à la colonne basse pression 29.
  • Un débit de liquide enrichi en oxygène 55, un débit intermédiaire 53 et un débit liquide riche en azote 51 sont soutirés de la colonne moyenne pression 27, refroidis dans l'échangeur 31, détendus et envoyés à des niveaux différents de la colonne basse pression 29.
  • De l'azote gazeux moyenne pression 49 est condensé dans un vaporiseur intermédiaire 35 de la colonne basse pression 29 et envoyé comme reflux en tête de la colonne moyenne pression 27. Un autre débit d'azote gazeux moyenne pression 47 se réchauffe dans la ligne d'échange.
  • De l'oxygène liquide 37, contenant au moins 80% mol. d'oxygène et éventuellement au plus 98% mol. d'oxygène, est soutiré en cuve de la colonne basse pression 29, pressurisé par une pompe 39 à une pression inférieure à 9 bars abs, voire inférieure à 5 bars abs et envoyé au vaporiseur 41. A part une purge de liquide 43, l'oxygène se vaporise dans le vaporiseur 41 par échange de chaleur avec la fraction d'air 11 à la pression P2. Cet oxygène forme ensuite le premier débit d'oxygène gazeux pressurisé 45 qui se réchauffe dans la ligne d'échange 21. La fraction d'air 11 se trouve partiellement condensée et est envoyée à la double colonne.
  • Le liquide de purge 43 est pressurisé jusqu'à une pression d'au moins 10 bars abs, ou d'au moins 15 bar abs, voire au moins 20 bars abs dans une pompe 63 puis se vaporise dans la ligne d'échange 21. Le deuxième débit gazeux ainsi produit 59 est envoyé à un stockage gazeux sous pression 3 et détendu pour être mélangé avec le débit 45 via la conduite 61.
  • Ici la vaporisation de liquide de purge s'effectue en utilisant principalement de la chaleur sensible, de sorte qu'aucun débit d'air sortant de l'échangeur 21 n'est totalement condensé, voire n'est condensé.
  • Alternativement comme illustré dans la Figure 2, le liquide de purge pressurisé 43 peut être vaporisé dans un échangeur auxiliaire 21A, distinct de la ligne d'échange, contre un débit d'air 25A et avec un débit de fluide frigorigène, par exemple un débit d'azote 57A se réchauffant du procédé de séparation.
  • Le débit 25A refroidi dans l'échangeur 21A se mélange avec le débit refroidi 25 et le débit d'azote 57A réchauffé dans l'échangeur 21A se mélange avec le débit réchauffé 57.
  • Le deuxième débit d'oxygène gazeux 59, 61 formé par la vaporisation peut être utilisé comme gaz de secours lors d'une interruption de la production d'oxygène gazeux 45.
  • Ainsi le seul débit d'air qui sert à vaporiser l'oxygène de purge 43 reste sous forme gazeuse dans l'échangeur 21A et la vaporisation se réalise par échange de chaleur sensible.
  • Pour toutes les figures, une quantité variable du deuxième débit d'oxygène gazeux est mélangée avec le premier débit afin de produire un débit mélangé substantiellement constant.
  • Cette quantité variable du liquide de purge vaporisé peut être mélangée au premier débit 45 pour lisser les variations de débits, dues, par exemple à des variations de la pression du réseau d'oxygène.
  • En détectant une réduction de pression dans la ligne 45, due, par exemple à une demande accrue d'oxygène, de l'oxygène peut être détendu et envoyé du stockage 3 vers la ligne 45 par la conduite 61.
  • En cas de panne de l'appareil de séparation d'air, le débit d'oxygène 45 réduira ou sera inexistant. Dans ce cas, le débit d'oxygène 63 du stockage 3 peut alimenter un client, le temps qu'un vaporiseur de secours se mette en marche pour éviter tout arrêt de production.
  • Le débit 37 est le seul débit contenant plus que 60% mol. d'oxygène soutiré de la colonne basse pression.
  • Le stockage 3 opère à une pression plus élevée que le débit 45.

Claims (9)

  1. Appareil de séparation d'air comprenant une double colonne comprenant une colonne moyenne pression (27) et une colonne basse pression (29), un échangeur principal (21), un vaporiseur (41), un compresseur principal (2), des moyens pour envoyer tout l'air à traiter dans la double colonne au compresseur principal pour produire de l'air substantiellement à la pression P1 de la colonne moyenne pression, des moyens (5) pour envoyer une partie de l'air substantiellement à une pression élevée P2 à l'échangeur principal et ensuite au vaporiseur, une conduite pour envoyer de l'air au moins partiellement condensé dans le vaporiseur à au moins une des colonnes, une conduite pour envoyer de l'air à la pression P1 à la colonne moyenne pression, des moyens de pressurisation (39) constitués par une première pompe, une conduite pour soutirer de l'oxygène liquide de la colonne basse pression et pour l'envoyer aux moyens de pressurisation, une conduite pour envoyer de l'oxygène liquide pressurisé à une pression inférieure à 9 bar abs des moyens de pressurisation au vaporiseur, une conduite pour envoyer de l'oxygène gazeux du vaporiseur à l'échangeur principal pour se réchauffer pour former un premier débit d'oxygène gazeux, caractérisé en ce qu'il comprend une deuxième pompe de liquide de purge (63), une conduite de purge pour envoyer de l'oxygène liquide de purge (43) du vaporiseur à la deuxième pompe de liquide de purge pour le pressuriser, la conduite de purge n'étant pas reliée à un stockage de liquide de purge, en ce qu'il comprend
    - soit une conduite pour envoyer l'oxygène pressurisé de la deuxième pompe à l'échangeur principal (21) pour se vaporiser et former un deuxième débit d'oxygène gazeux,
    - soit un échangeur (21A) distinct de l'échangeur principal et une conduite pour envoyer l'oxygène pressurisé de la deuxième pompe à l'échangeur pour se vaporiser et former un deuxième débit d'oxygène gazeux
    en ce qu'il comprend une conduite d'air comprimé reliée au compresseur principal et à une conduite reliée à la double colonne, l'échangeur principal ou selon le cas l'échangeur étant relié à la conduite d'air comprimé reliée au compresseur principal et à la conduite reliée à la double colonne, et en ce qu'il comprend un stockage gazeux sous pression (3) relié à l'échangeur (21, 21A) de vaporisation d'oxygène de purge pour recueillir l'oxygène gazeux.
  2. Appareil suivant la revendication 1 dans lequel l'échangeur (21, 21A) comprend des passages reliés à une conduite d'amenée d'air d'alimentation et des passages reliés à une conduite d'amenée de fluide frigorigène, provenant éventuellement de la double colonne.
  3. Procédé de séparation d'air dans un appareil comprenant une double colonne comprenant une colonne moyenne pression (27) et une colonne basse pression (29), un échangeur principal (21), un vaporiseur (41), un compresseur principal (2) et des moyens de pressurisation (43) constitués par une première pompe, dans lequel on envoie tout l'air à traiter dans la double colonne au compresseur principal pour produire de l'air substantiellement à la pression P1 de la colonne moyenne pression, on envoie une partie de l'air substantiellement à une pression élevée P2 à l'échangeur principal et ensuite au vaporiseur, on envoie de l'air au moins partiellement condensé dans le vaporiseur à au moins une des colonnes, on envoie de l'air à la pression P1 à la colonne moyenne pression, on soutire de l'oxygène liquide de la colonne basse pression et on le pressurise, on envoie de l'oxygène liquide pressurisé à une pression inférieure à 9 bar abs au vaporiseur et on envoie un premier débit d'oxygène gazeux du vaporiseur à l'échangeur principal pour se réchauffer caractérisé en ce que l'appareil comprend une deuxième pompe de liquide de purge (63) et en ce que on pressurise de l'oxygène liquide de purge (43) du vaporiseur dans la deuxième pompe de liquide de purge, l'oxygène liquide de purge est pressurisé sans avoir été stocké et ensuite est vaporisé dans un échangeur qui est l' échangeur principal (21) ou un échangeur (21A) distinct de l'échangeur principal par échange de chaleur avec de l'air, comprimé dans le compresseur principal et destiné à la double colonne, pour former un deuxième débit d'oxygène gazeux et le deuxième débit d'oxygène gazeux est envoyé à un stockage gazeux sous pression (3) et sert de production de secours.
  4. Procédé selon la revendication 3 dans lequel l'oxygène de purge (43) est pressurisé à une pression d'au moins 10 bars abs, de préférence au moins 15 bars abs, voire au moins 20 bars abs dans la deuxième pompe (63).
  5. Procédé selon l'une des revendications 3 ou 4 dans lequel une quantité variable du deuxième débit d'oxygène gazeux (61) est mélangée avec le premier débit (45) d'oxygène gazeux afin de produire un débit mélangé substantiellement constant.
  6. Procédé selon l'une des revendications 3 à 5 dans lequel l'oxygène liquide (37) soutiré de la colonne basse pression (29) contient au moins 80% mol. d'oxygène.
  7. Procédé selon la revendication 6dans lequel l'oxygène liquide (37) soutiré de la colonne basse pression (29) constitue le seul débit contenant au moins 80% mol. d'oxygène soutiré de la colonne basse pression.
  8. Procédé selon l'une des revendications 3 à 7 dans lequel l'oxygène liquide (37) soutiré de la colonne basse pression (29) contient au plus 98% mol. d'oxygène.
  9. Procédé selon l'une des revendications 3 à 8 dans lequel aucun débit d'air ne se condense entièrement, voire ne se condense dans l'échangeur (21, 21A) où se vaporise l'oxygène de purge (43).
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CN104067079A (zh) 2014-09-24
CA2828716A1 (fr) 2012-09-27
FR2972794B1 (fr) 2015-11-06
AU2012230171B2 (en) 2017-03-30
ES2859549T3 (es) 2021-10-04
WO2012127148A3 (fr) 2014-12-04
FR2972794A1 (fr) 2012-09-21
US20130340476A1 (en) 2013-12-26
ZA201306723B (en) 2015-03-25
EP2686628A2 (fr) 2014-01-22

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