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EP2026024A1 - Procédé et dispositif pour la production d'argon par séparation cryogénique d'air - Google Patents

Procédé et dispositif pour la production d'argon par séparation cryogénique d'air Download PDF

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Publication number
EP2026024A1
EP2026024A1 EP08012054A EP08012054A EP2026024A1 EP 2026024 A1 EP2026024 A1 EP 2026024A1 EP 08012054 A EP08012054 A EP 08012054A EP 08012054 A EP08012054 A EP 08012054A EP 2026024 A1 EP2026024 A1 EP 2026024A1
Authority
EP
European Patent Office
Prior art keywords
condenser
column
argon column
passages
crude argon
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.)
Withdrawn
Application number
EP08012054A
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German (de)
English (en)
Inventor
Horst Corduan
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Priority claimed from DE102007035619A external-priority patent/DE102007035619A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP08012054A priority Critical patent/EP2026024A1/fr
Publication of EP2026024A1 publication Critical patent/EP2026024A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • F25J3/04333—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
    • F25J3/04357—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 and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • 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
    • F25J3/04624—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 integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2210/04—Mixing or blending of fluids with the feed 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/58—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being argon or crude argon
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
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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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
    • 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 invention relates to a method according to the preamble of patent claim 1.
  • the distillation column system for nitrogen-oxygen separation of the invention may be formed as a single column system for nitrogen-oxygen separation, as a two-column system (for example as a classic Linde double column system), or as a three or more column system.
  • further steps for obtaining other air components may be provided in the method, in particular further noble gases.
  • the "crude argon column” within the meaning of the claim is used for argon-oxygen separation.
  • the crude argon column may be formed by a one-piece column or by a two- or multi-part column, as in EP 628777 B1 is described.
  • the "pure argon column” is used for argon-nitrogen separation.
  • the "crude argon stream” has a higher argon concentration than the "argon-containing stream”.
  • the "pure argon product stream” has a higher argon concentration than crude argon stream and is preferably withdrawn from the bottom of the pure argon column, for example from its bottom.
  • Processes for argon recovery of the type mentioned are, for example DE 2325422 A .
  • EP 942246 A2 EP 1103772 A1 .
  • the invention has for its object to provide a method of the type mentioned above and a corresponding device, which are economically particularly favorable to operate by having an increased product yield, higher product purity, lower operating costs and / or lower investment costs.
  • top condenser of the crude argon column is designed as a reflux condenser and top gas of the crude argon column is introduced into the return passages of the reflux condenser.
  • lux condenser also called dephlegmator
  • dephlegmator a heat exchanger having return passages. These return passages are pressurized from below with steam (here: overhead gas of the crude argon column). This condenses at least partially when ascending in the return passages.
  • the return passages are designed so that the condensed liquid is not entrained, but flows down. Due to the countercurrent of vapor and liquid, a rectification takes place in the return passages.
  • the condensate, which exits at the lower end, is enriched in less volatile components, the steam exiting overhead is more volatile.
  • the heat exchanger block (or even a plurality of heat exchanger blocks) may be arranged inside a pressure vessel, as described, for example, in US Pat EP 1189000 A2 is shown, or the heat exchanger block is completed on all sides by headers, see for example US 6128920 .
  • the reflux condenser in the head of a separation column here: the crude argon column
  • the return passages are at its lower end in communication with the upper region of the separation column, see German patent application 102006037058 and corresponding applications.
  • the one or more heat exchanger blocks of the reflux condenser are preferably designed as a plate heat exchanger, in particular as a brazed aluminum plate heat exchanger.
  • a reflux condenser not only allows heat exchange, but also mass transfer between the gas rising in the return passages and the liquid flowing down there, similar to the corrugated packings of a mass transfer column.
  • This release effect can be expressed as the HETP value (Height Equivalent to One Theoretical Plate).
  • the HETP value of the capacitor is in the range of 300 to 600 mm.
  • a 1.5 m high reflux condenser acts like up to five theoretical plates.
  • this effect does not affect the argon-oxygen separation at the top of the crude argon column, ie the use of the reflux condenser does not save mass transfer elements (practical trays, ordered packing or disordered packing) in the crude argon column.
  • the upper area of the argon column is off US 5133790 is not used for argon-oxygen separation (as in the crude argon column of the invention), but for argon nitrogen separation, which in the Method of the type mentioned is carried out practically exclusively in the pure argon column.
  • Such capacitors are regularly designed as a condenser-evaporator. Against the condensing on the liquefaction side (return passages) head gas thus a cooling fluid is evaporated on the evaporation side.
  • the heat exchanger block is usually arranged in a bath. Because of the hydrostatic pressure, the temperature in the evaporation passages rises from top to bottom.
  • the gas flowing upwards in the return passages becomes increasingly nitrogen-rich and is the coldest at the top of the condenser because of the increased nitrogen content (see FIG. 4 ).
  • the temperature profile in the return passages adapts to those of the evaporation passages.
  • the return condenser creates a natural tendency for a driving temperature gradient which remains almost constant over the entire block height.
  • the driving temperature gradient in the lower capacitor area is always much smaller than in the upper area. This weakens the contribution of the heating surface located in the lower part of the condenser to the total heat exchange.
  • the temperature difference between evaporation and liquefaction passages is almost constant.
  • the exchange losses can be reduced, or the exchange area is reduced accordingly, thus reducing the investment costs.
  • the liquid cooling fluid is supplied to the evaporation passages at its lower end and the mixture of vaporized cooling fluid and liquid remaining cooling fluid is withdrawn from the lower end of the evaporation passages.
  • the top condenser may be formed as a bath evaporator, in which the evaporation passages are open at the top and bottom and the cooling fluid is guided by the thermosiphon effect from bottom to top through the evaporation passages.
  • the top condenser is formed by exactly one plate heat exchanger block.
  • the crude argon stream is withdrawn from the upper region of the return passages.
  • the gas fraction remaining after flowing through has a particularly high argon concentration and its oxygen content is particularly low.
  • the crude argon stream thus also contains a relatively large amount of nitrogen; However, this can be separated easily in the pure argon column.
  • no residual gas stream is withdrawn from the upper region of the crude argon column and from the reflux passages.
  • no further stream is withdrawn from the upper region, including the return passages, in addition to the crude argon stream.
  • the crude argon column is drained of just another stream which is returned to the nitrogen-oxygen separation distillation column system (for example, the low-pressure column of a two-column system from which the argon-containing stream is withdrawn).
  • the crude argon stream of the crude argon column or the top condenser is taken off in gaseous form and at least partially, for example completely condensed, upstream of its introduction into the pure argon column in an additional condenser.
  • the crude argon stream can be introduced at least partially, for example completely in liquid form, into the pure argon column.
  • the top condenser and the additional condenser are designed as a condenser-evaporator, wherein both evaporation passages are fed with the same cooling fluid.
  • the cooling fluid is partially vaporized in the evaporation passages, whereby liquid is entrained by the thermosiphon effect and returned to the liquid bath.
  • oxygen-enriched liquid from the distillation column system is used for nitrogen-oxygen separation, such as from the bottom of the high-pressure column of a two-column system.
  • top condenser and the additional condenser are designed as liquid bath evaporators and are arranged in the same liquid bath. Since the additional capacitor regularly has a lower height than the top condenser, the additional condenser can still be operated with a temperature at the lower end, which is lower than the temperature at the lower end of the top condenser.
  • a residual gas stream is withdrawn from the head of the pure argon column or from the upper region of the return passages and mixed with the feed air, in particular before its compression.
  • This recycling of the residual gas from the head of the pure argon column or the crude argon column can also be used with advantage in argon recovery processes without reflux condenser at the top of the crude argon column.
  • the argon contained in it is returned to the process. The argon yield increases accordingly.
  • the invention also relates to a device according to claims 12 to 15.
  • atmospheric air 1 is sucked in via a filter 2 from an air compressor 3 and there compressed to an absolute pressure of 5.0 to 7.0 bar, preferably about 5.5 bar and is then in a direct contact cooler 4 in direct heat exchange with cooling water 5, 6 cooled, which originates (1) from an evaporative cooler 7, on the other hand (6) is supplied from an external source.
  • the compressed and cooled air 8 is cleaned in a cleaning device 9 having a pair of containers filled with adsorbent material, preferably molecular sieve.
  • the purified air 10 is cooled in a main heat exchanger system 11 a, 11 b, 11 c to about dew point.
  • the cold air 12 is introduced into the high-pressure column 13 of a distillation column system for nitrogen-oxygen separation, which also has a low-pressure column 14.
  • High-pressure column 13 and low-pressure column 14 are designed as classic Linde double column and are connected via a main condenser 15 in heat exchanging connection.
  • the operating pressures - at the top - are 4.5 to 6.5 bar, preferably about 5.0 bar in the high pressure column and 1.2 to 1.7 bar, preferably about 1.3 bar in the low pressure column.
  • Liquid raw oxygen 16 is withdrawn from the sump of the high-pressure column 13, supercooled in a supercooling countercurrent 17 and further cooled to a part 19 in a sump evaporator 21 of the pure argon column 20.
  • Another part 22 can be passed past the bottom evaporator 21.
  • a part 23 flows into the evaporation space of a top condenser 24 of a crude argon column 25, another part in the evaporation space of a top condenser 27 of the pure argon column 20.
  • the in the top condensers 24, 27 evaporated crude oxygen 28, 29 via line 30 of the low pressure column 14 at a first Supplied intermediate point.
  • the remaining liquid portion 31 from the top condenser 24 of the crude argon column 25 is also guided to the first intermediate point of the low-pressure column 14.
  • the remaining liquid portion 32 from the top condenser 27 of the pure argon column 20 is fed to a second intermediate point of the low-pressure column 14, which is above the first intermediate point.
  • Gaseous nitrogen 33 from the head of the high pressure column 13 is directed to a first portion 34 to the cold end of the main heat exchanger 11a where it is warmed to about ambient temperature and then divided into a pressurized product stream 36 (GAN I) and a recycle stream 37.
  • the circulation stream 37 is compressed in a cycle compressor 38 with aftercooler 39 to a pressure of 25 to 60 bar, preferably about 35 bar, and cooled in the main heat exchanger 11a.
  • a portion 40 of the high-pressure nitrogen is removed from the main heat exchanger at an intermediate temperature and expanded in an expansion turbine 41 to approximately high-pressure column pressure.
  • the relaxed circulation stream 42 is again admixed with the cold product stream 34. Any existing liquid is previously separated (43) and fed via line 44 to the top of the low pressure column 14. Another part 61 of the high pressure nitrogen is led to the cold end of the main heat exchanger 11a and then abandoned on the high-pressure column 13.
  • the remaining gaseous top nitrogen 45 of the high-pressure column 13 is at least partially condensed in the main condenser 15.
  • the generated during this process liquid nitrogen 46 is given to a part 47 of the high-pressure column 13 as reflux.
  • Another part 48, 49 is passed to the head of the low-pressure column 14 after subcooling in the subcooling countercurrent 17.
  • a part 50 can be deducted as liquid nitrogen product (LIN).
  • gaseous oxygen 51 is removed, warmed in the main heat exchanger 11a and withdrawn via line 52 as a non-pressurized gaseous product (GOX III).
  • a liquid oxygen stream 53 from the bottom of the low pressure column 14 is supercooled in the subcooling countercurrent 17 and fed via line 54 to a liquid tank (LOX).
  • At least a portion of the liquid oxygen is withdrawn via line 55 to the tank again, brought in a pump 56 to the required product pressure, for example 6 to 60 bar, preferably about 31 bar, and vaporized in the main heat exchanger 11a against high pressure nitrogen (or pseudo at supercritical pressure -Vaporated) and warmed to ambient temperature and finally withdrawn via line 57 as a gaseous high pressure product (GOX I).
  • a portion 58 of the high-pressure liquid is expanded via a throttle valve 59 to an intermediate pressure of, for example, 6 to 25 bar, preferably about 15 bar and evaporated under this lower pressure and withdrawn via line 60 as gaseous medium pressure product (GOX II).
  • Gaseous nitrogen 62, 63, 64 from the head of the low pressure column 14 and gaseous impurity 65, 66, 67 from an intermediate point of the low pressure column 14 are respectively supercooled in the subcooling countercurrent 17, warmed in the main heat exchanger blocks 11 c and 11 b and via line 68 - If necessary, after heating 69 - used as a regeneration gas for the cleaning device 9, fed via line 70 to the evaporative cooler 70 and / or blown off via line 71 directly into the atmosphere.
  • an argon-containing stream 72 is taken from the low-pressure column 14 and fed to the crude argon column 25 directly above the sump.
  • the crude argon column 25 is made in one piece in this example. Bottom liquid 73 of the crude argon column is returned via pump 74 and line 75 into the low-pressure column.
  • the top condenser 24 of the crude argon column 25 is designed according to the invention as a reflux condenser. Gas from the top of the crude argon column 25 flows down into the return passages where it is partially condensed. The condensate generated in this case flows in countercurrent to the rising gas in the return passages down and is used in the crude argon column 25 as a liquid reflux. On the evaporation side, the top condenser 24 is designed as a bath condenser.
  • the cooling fluid which is formed here by liquid crude oxygen 23, flows in at the bottom via one or more lateral openings into the evaporation passages and is partially evaporated there.
  • Liquid is entrained by the thermosiphon effect, exits along with the vaporized portion at the top of the evaporation passages, and is returned to the liquid bath.
  • the top condenser is thus formed on the evaporation side as a bath evaporator.
  • a crude argon stream 76 is taken off in gaseous form via a lateral header and fed to the pure argon column 20 at an intermediate point.
  • the top condenser of the pure argon column 20 is conventionally designed in the example on the liquefaction side, that is, the head gas 77 of the pure argon column 20 flows from top to bottom through the liquefaction passages.
  • the top condenser 27 of the pure argon column 20 and / or the main condenser 15 could be designed as reflux condenser.
  • a residual gas stream 78 is withdrawn and blown off into the atmosphere in the example. Alternatively it can be returned to the distillation column system for nitrogen-oxygen separation or to the air compressor 3 via its own blower.
  • the bottom liquid 79 of the pure argon column 20 is vaporized to a part 80 in the bottom evaporator 21 and the generated thereby vapor 81 is as Ascending gas used in the pure argon column 20. The remainder is taken as a liquid pure argon product stream 82.
  • FIG. 2 gives way before all in the execution of pure argon column 20 of FIG. 1 from.
  • the pure argon column has no top condenser here.
  • the crude argon stream 176 is here formed by a part of the return passages of the top condenser 24 of the crude argon column 25 and fed to the top of the pure argon column 20.
  • the top gas 177 of the pure argon column 20 is returned to the top of the crude argon column 25.
  • the residual gas stream 178 is formed by the uncondensed in the top condenser 24 portion of the top gas of crude argon and pure argon. It is removed at the upper end of the return passages via a lateral header and, like the residual gas stream 78 of the FIG. 1 be treated.
  • FIG. 3 shows only the crude argon column 25 and the pure argon column 20. Otherwise, the method is identical to those of FIGS. 1 and 2 , Similar to FIG. 2 Here is a first Rohargonstrom 276a liquid introduced into the pure argon column 20. Deviating from FIG. 2 However, this introduction is not done on the head, but as in FIG. 1 at an intermediate point of the pure argon column 20. At this point, a part 277 of the ascending in the pure argon gas and withdrawn to the top of the crude argon column 25.
  • the vapor 276b from the head of the return passages of the top condenser 24 forms a second crude argon stream.
  • This is at least partially condensed in an additional capacitor 227, which is designed as a condenser-evaporator.
  • the condensate 282 is given as reflux to the top of the pure argon column.
  • the evaporation side of the additional capacitor 227 is like that of the top condenser 24 formed as a liquid bath evaporator, both preferably being arranged in the same liquid bath, which is fed by liquid crude oxygen 23.
  • the temperature profile is plotted against the height of the condenser block (left axis). Between the liquid condensing in the return passages whose temperature is approximately equal to the temperature in the evaporation passages (upper curve “condensation”) and in countercurrent For ascending evaporating gas (lower curve “evaporation”) there is a temperature difference (MTD), which is almost constant over the height of the reflux condenser.
  • MTD temperature difference
  • the reflux condenser has assumed in the example a separation effect of five theoretical plates.
  • a theoretical bottom causes in the top condenser of a crude argon column a nitrogen increase by a factor of about 3 (K value of nitrogen in argon).
  • All described capacitors are preferably designed as soldered aluminum plate heat exchangers whose channels contain corrugated sheets, so-called fins.
  • fins Within the return passages basically the same types of fins can be used. However, it may be beneficial in reflux condensers to use different Fintypen.
  • An embodiment is in FIG. 5 shown.
  • the return passages shown here are divided into four sections A to D, in which different types of fins are used.
  • the gas load and thus the flood tendency is greatest.
  • the gas load is getting smaller. Therefore, in the lower region A, a fin with a small specific pressure loss and a relatively poor heat transfer is preferably selected.
  • FIG. 6 shows a further method to make the operation of the return passages of the reflux condenser 24 so that the basically upward decreasing gas load is compensated.
  • a part of the gas to be condensed is given up on the return passages. This reduces the gas load in the lower zone. Since the amount of gas flowing to the head is only a subset of the amount of gas to be condensed, the necessary piping takes up less space and construction volume is saved.
  • the reflux condenser on the evaporation side is designed as a falling-film evaporator, that is to say vaporizing cooling fluid is added at the top and flows down in a film flow through the evaporation passages.
  • vaporizing cooling fluid is added at the top and flows down in a film flow through the evaporation passages.

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EP2458311A1 (fr) 2010-11-25 2012-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un produit d'impression gazeux par décomposition à basse température d'air
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2520886A1 (fr) 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
EP2568242A1 (fr) 2011-09-08 2013-03-13 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'acier
EP2600090A1 (fr) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
WO2014135271A2 (fr) 2013-03-06 2014-09-12 Linde Aktiengesellschaft Installation de séparation d'air, procédé de récupération d'un produit contenant de l'argon et procédé pour créer une installation de séparation d'air
EP2784420A1 (fr) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
WO2014169989A1 (fr) * 2013-04-18 2014-10-23 Linde Aktiengesellschaft Dispositif de post-équipement pour la décomposition d'air à basse température, installation de post-équipement et procédé de post-équipement d'une installation de décomposition d'air à basse température
EP2801777A1 (fr) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
EP2963369A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963371A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
EP2963370A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2458311A1 (fr) 2010-11-25 2012-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un produit d'impression gazeux par décomposition à basse température d'air
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2466236A1 (fr) 2010-11-25 2012-06-20 Linde Aktiengesellschaft Procédé de production d'un produit d'impression gazeux par décomposition à basse température de l'air
EP2520886A1 (fr) 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
EP2568242A1 (fr) 2011-09-08 2013-03-13 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'acier
DE102011112909A1 (de) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
EP2600090A1 (fr) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
WO2014135271A2 (fr) 2013-03-06 2014-09-12 Linde Aktiengesellschaft Installation de séparation d'air, procédé de récupération d'un produit contenant de l'argon et procédé pour créer une installation de séparation d'air
EP2784420A1 (fr) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
WO2014169989A1 (fr) * 2013-04-18 2014-10-23 Linde Aktiengesellschaft Dispositif de post-équipement pour la décomposition d'air à basse température, installation de post-équipement et procédé de post-équipement d'une installation de décomposition d'air à basse température
CN105264317A (zh) * 2013-04-18 2016-01-20 林德股份公司 空气低温分离的改造装置、改造系统以及改造低温空气分离系统的方法
CN105264317B (zh) * 2013-04-18 2019-02-12 林德股份公司 空气低温分离的改造装置、改造系统以及改造低温空气分离系统的方法
EP2801777A1 (fr) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
EP2963369A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963371A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
EP2963370A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
WO2016005031A1 (fr) 2014-07-05 2016-01-14 Linde Aktiengesellschaft Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable

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