EP3040665A1 - Système de colonne de distillation et installation pour la production d'oxygène par séparation cryogénique de l'air - Google Patents

Système de colonne de distillation et installation pour la production d'oxygène par séparation cryogénique de l'air Download PDF

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Publication number
EP3040665A1
EP3040665A1 EP14004443.9A EP14004443A EP3040665A1 EP 3040665 A1 EP3040665 A1 EP 3040665A1 EP 14004443 A EP14004443 A EP 14004443A EP 3040665 A1 EP3040665 A1 EP 3040665A1
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Prior art keywords
column
distillation column
air
pressure
heat exchanger
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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.)
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EP14004443.9A
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German (de)
English (en)
Inventor
Anton Moll
Dimitri Goloubev
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Linde GmbH
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Linde GmbH
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Priority to EP14004443.9A priority Critical patent/EP3040665A1/fr
Publication of EP3040665A1 publication Critical patent/EP3040665A1/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
    • F25J3/04642—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
    • F25J3/04006—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
    • F25J3/04084—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—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.
    • 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
    • F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
    • F25J3/04909—Structured packings
    • 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
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • 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
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the 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
    • 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
    • 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
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Definitions

  • the invention relates to a distillation column system for the production of oxygen by cryogenic separation of air according to the preamble of patent claim 1.
  • the distillation column system of the invention can basically be designed as a classic two-column system with high-pressure column and low-pressure column. In addition to the two separation columns for nitrogen-oxygen separation, it can have other devices for obtaining other air components, in particular noble gases, for example krypton-xenon recovery.
  • the main capacitor is formed in the invention as a condenser-evaporator.
  • a condenser-type evaporator is a heat exchanger in which a first, condensing fluid stream undergoes indirect heat exchange with a second, evaporating fluid stream.
  • Each condenser-evaporator has a liquefaction space and an evaporation space consisting of liquefaction passages or evaporation passages the condensation (liquefaction) of a first fluid stream is carried out, in the evaporation space the evaporation of a second fluid stream.
  • Evaporation and liquefaction space are formed by groups of passages which are in heat exchange relationship with each other.
  • argon discharge column here refers to a separation column for argon-oxygen separation, which does not serve for obtaining a pure argon product but for discharging argon from the air to be separated into the high-pressure column and low-pressure column.
  • Their circuit differs only slightly from that of a classical crude argon column, which generally contains 70 to 180 theoretical plates; however, it contains significantly less theoretical plates, namely less than 40, in particular between 15 and 35.
  • an argon discharge column Like a crude argon column, the bottom portion of an argon discharge column is connected to an intermediate point of the low pressure column, and the argon discharge column is cooled by a top condenser, on the evaporation side of which relaxed bottoms are removed High-pressure column is initiated; an argon discharge column has no bottom evaporator.
  • the distillation column system of an air separation plant is arranged in one or more cold boxes.
  • a "cold box” is here understood to mean an insulating casing which comprises a heat-insulated interior completely with outer walls; in the interior are arranged to be isolated plant parts, for example, one or more separation columns and / or heat exchangers.
  • the insulating effect can be effected by appropriate design of the outer walls and / or by the filling of the gap between system parts and outer walls with an insulating material. In the latter variant, a powdery material such as perlite is preferably used.
  • Both the distillation column system for nitrogen-oxygen separation of a cryogenic air separation plant and the main heat exchanger and other cold plant parts must be enclosed by one or more cold boxes.
  • the outer dimensions of the coldbox usually determine the transport dimensions of the package in prefabricated systems.
  • a "main heat exchanger” serves to cool feed air in indirect heat exchange with recycle streams from the distillation column system. It can be composed of a single or several parallel and / or serially connected Heat exchanger sections may be formed, for example, from one or more plate heat exchanger blocks. Separate heat exchangers which specifically serve to vaporize or pseudo-evaporate a single liquid or supercritical fluid without heating and / or vaporization of another fluid, do not belong to the main heat exchanger. Such a separate heat exchanger can be formed for example by a secondary condenser or by a separate heat exchanger for evaporation or pseudo-evaporation and optionally heating a liquid stream under elevated pressure or a supercritical flow.
  • Some air separation plants include, for example, in addition to the main heat exchanger, a secondary condenser or a high-pressure exchanger for evaporation or pseudo-evaporation and optionally heating liquid product placed on pressure against a high pressure air stream, which is formed by a portion of the feed air.
  • a secondary condenser and such a high-pressure exchanger are not considered here as part of the main heat exchanger.
  • top, bottom, “above”, “below”, “above”, “below” etc. refer here to the spatial orientation of the separation columns in normal operation.
  • An arrangement of two columns “one above the other” is understood here to mean that the upper end of the lower of the two columns is at lower or the same geodetic height as the lower end of the upper of the two columns and the projections of the two columns in a horizontal plane overlap.
  • the two columns are arranged exactly one above the other, that is, the axes of the two columns extend on the same vertical line.
  • a distillation column system of the type mentioned above with argon discharge column is made US 5235816 known.
  • Such systems are prefabricated regularly as far as possible in the production, the pre-embarrassed parts are transported to the site and finally connected there.
  • the entire double column can be transported with its coldbox. If the size of the system no longer allows this, the double column - if necessary in two parts - is transported without coldbox and piping.
  • An additional pillar like that Argon discharge column causes additional effort with its own coldbox. This column is brought separately to the site and connected there with relatively great effort on site with the rest of the system. In order to avoid an additional cryogenic pump, this column is placed (in its own cold box) on an elaborate frame. This position causes, among other things, increased space requirements for the entire plant ("plant footprint").
  • the invention has for its object to make a distillation column system of the type mentioned as compact as possible and to simplify its construction.
  • the argon discharge column is placed over the double column.
  • the axes of Argonausschleusklaner and low pressure column lie on a straight line.
  • the complete distillation column system can be prefabricated in the workshop;
  • the argon discharge column does not need to be transported separately and requires only minimal assembly work on the construction site.
  • the transport of a combination of double column and argon discharge column is in practice not much more complex than that of the double column alone (provided the logistics allow the slightly increased transport length).
  • the additional argon discharge column can in many cases be transported together with the low-pressure column.
  • the pressure column is usually transported separately together with the main condenser tank.
  • Another significant advantage is that the elaborate frame for the Argonausschleuskla and a separate coldbox is no longer needed.
  • the low-pressure column contains mass transfer elements which are formed in at least a portion of the low-pressure column by an ordered packing, which is made of folded metal sheets, wherein the ordered packing has a specific surface area of more than 1000 m 2 / m 3 , in particular of 1200 m 2 / m 3 or more.
  • an ordered package particularly high density in the low-pressure column used.
  • part of the mass transfer region of the low-pressure column may be filled with a particularly dense packing (and the remainder for example by packing of lower density or else by a combination of packing and conventional rectification trays), or all mass transfer elements are formed by the particularly dense packing.
  • an ordered packing preferably with more than 700 or 1000 m 2 / m 3 , or sieve trays or a combination of these two types of mass transfer elements are used.
  • the use of relatively high specific gravity packing is advantageous, the argon discharge column containing mass transfer elements formed in at least a portion of the low pressure column through an ordered packing made of folded metal sheets, the ordered packing having a specific surface area of more than 700 m 2 / m 3 , in particular of 1200 m 2 / m 3 or more.
  • the entire mass transfer region of the argon discharge column is equipped with packing of such high density.
  • the main capacitor is arranged in the bottom region of the low-pressure column.
  • the main condenser is below the mass transfer elements of the low pressure column in the same container as this.
  • the main condenser could be located in a separate container from the low pressure column.
  • the invention also relates to a plant for the production of oxygen by cryogenic separation of air according to claim 7 with a main air compressor, an air pre-cooling unit, an air cleaning unit and a main heat exchanger and two of the distillation column systems described above, both receiving feed air from the common main heat exchanger.
  • the apparatuses upstream of the two distillation column systems may in particular be formed by a single pre-cooling, a single air cleaning and / or a single main heat exchanger.
  • At least a portion of the feed air for both distillation column systems can be cooled together in the main heat exchanger and withdrawn from the main heat exchanger in a total compressed air line.
  • the total compressed air line is then branched into the first compressed air sub-flow line to the first distillation column system and the second compressed air sub-flow line to the second distillation column system.
  • a system according to the invention has a high-pressure exchanger in addition to the main heat exchanger, then this is likewise used for both distillation column systems, ie the high-pressure cold air from the high-pressure exchanger is distributed to the two distillation column systems and the product stream intended for the high-pressure exchanger becomes liquid from both distillation columns -Systems removed, merged and sent to the high pressure exchanger.
  • the main heat exchanger usually consists anyway of several parallel blocks. Then it is advisable to divide the blocks into two symmetrical groups in order to better control the main heat exchanger.
  • air to be separated and the corresponding stream of impure nitrogen from the same distillation column system are passed through the first exchanger group.
  • the second group the corresponding currents flow for or from the second distillation column system.
  • the remaining streams are distributed evenly over the blocks of both groups.
  • first distillation column system and the second distillation column system have the same size and in particular high-pressure column, low-pressure column and argon discharge column are the same size.
  • a “same size” is understood here to mean that the corresponding column heights and diameters do not differ from each other by more than 10%, in particular not more than 5%.
  • the comparison relates in pairs to the corresponding sections of the first and second high-pressure columns, the first and the second low-pressure columns or the argon discharge column n.
  • the two distillation column systems (each double column plus argon discharge column) can each be housed in a separate coldbox.
  • the first and the second distillation column system are arranged in a common coldbox.
  • the two distillation column systems are preferably operated independently of each other, but the warm plant parts and the main heat exchanger and optionally a high-pressure exchanger are shared.
  • both distillation column systems each have a separate subcooling countercurrent which is operable independently of the subcooling countercurrent of the other distillation column system, and in particular is not connected to piping to or from the other distillation column system.
  • the invention therefore also relates to a multi-stranded plant for the production of oxygen by cryogenic separation of air according to claim 15, wherein at least two of the strands are formed by the two of the plants described above, each with two distillation column systems.
  • a total capacity can be achieved which corresponds to a conventional five-strand plant.
  • a total capacity can be achieved which corresponds to a conventional five-strand plant.
  • five strands according to the invention suffice.
  • EP 1672301A1 US 7516626 B2 known in itself.
  • FIG. 1 is a plant with two distillation column systems shown.
  • the first distillation column system of the embodiment of the FIG. 1 has a first high pressure column 101, a first low pressure column 102, a first main condenser 103, and a first argon discharge column 152.
  • a second High pressure column 201, a second low pressure column 202, a second main condenser 203 and a second argon discharge column 252 belong to the second distillation column system of Figs FIG. 1 illustrated plant.
  • the inventive distillation column system may be equipped with any turbine configuration for the purpose of refrigeration.
  • FIG. 1 is, for example, the combination of a medium-pressure turbine (air is working to high-pressure column pressure relaxed) and a turbine injection (air is working to relax at low pressure column pressure) shown.
  • a pressure GAN turbine work-performing expansion of gaseous nitrogen from the high-pressure column to just above atmospheric pressure
  • a combination of injection turbine and pressure GAN turbine instead of the injection turbine.
  • the main condensers 103, 203 are formed in the example by two three-stage cascade evaporators.
  • the pairs of columns 101/102, 201/202 are arranged in the form of two double columns, the argon discharge column 152/252 according to the invention above.
  • Each of the two distillation column systems is independently regulated.
  • the pressure in the low-pressure columns for example, can be set and controlled separately. Through this decoupling, the overall control effort is made easier and any manufacturing tolerances in both double columns can be better compensated.
  • the system shown has an atmospheric air inlet filter 302, a main air compressor 303, an air pre-cooling unit 304, an air cleaning unit 305 (typically formed by a pair of molecular sieve adsorbers), a Booster Air Compressor 306 with aftercooler 307, and a main heat exchanger 308.
  • the main heat exchanger 308 is housed in its own coldbox, which is separate from the coldbox (s) around the distillation column systems.
  • a total compressed air flow 99 from the cold end of the main heat exchanger 308 is branched into a first compressed air partial flow 100 and a second compressed air partial flow 200.
  • the first compressed air sub-stream 100 is in the first high-pressure column 101, the second compressed air partial stream 200 introduced into the second high-pressure column 201.
  • the air recompressed in the final compressor 306 to its final pressure is liquefied in the main heat exchanger 308 (or, if its pressure is supercritical, pseudo-liquefied) and fed via line 311 to the distillation column systems where it branches into the streams 111 and 112.
  • a first nitrogen gas stream 104, 114 from the first high-pressure column 101 is introduced into the liquefaction space of the first main condenser 103.
  • liquid nitrogen 115 is generated, which is passed to at least a first part as a first liquid nitrogen stream 105 to the first high-pressure column 101.
  • a second nitrogen gas stream 204, 214 from the second high-pressure column 201 is introduced into the liquefaction space of the second main condenser 203.
  • liquid nitrogen 215 is generated, which is passed to at least a first part as a second liquid nitrogen flow 205 to the second high-pressure column 201.
  • a first liquid oxygen stream 106 from the first low-pressure column 102 flows from the lower end of the lowermost mass transfer layer 107 of the first low-pressure column 102 and is thereby introduced into the evaporation space of the first main capacitor 103.
  • gaseous oxygen is formed in the evaporation space of the first main capacitor 103. It is introduced at least to a first part as the first oxygen gas stream 108 in the first low pressure column 102 by flowing from below into the bottom mass transfer layer 107 of the first low-pressure column 102; if necessary, a second part can be obtained directly as a gaseous oxygen product and heated in the main heat exchanger 308.
  • a second liquid oxygen stream 206 from the second low-pressure column 202 flows from the lower end of the lowermost mass transfer layer 207 of the second low-pressure column 202 and is thereby introduced into the evaporation space of the second main condenser 203.
  • gaseous oxygen is formed in the evaporation space of the second main capacitor 203. He will at least become a first part as a second oxygen gas stream 208 introduced into the second low-pressure column 202 by flowing from below into the bottom mass transfer layer 207 of the second low-pressure column 202; if necessary, a second part can be obtained directly as a gaseous oxygen product and heated in the main heat exchanger 308.
  • the reflux liquids 109, 209 for the two low-pressure columns 102, 202 are each formed by a nitrogen-enriched liquid 120, 220, which is withdrawn at both high-pressure columns 101, 201 from an intermediate point (or alternatively directly from the head) and cooled in sub-coolers 123, 223. From the top of both low-pressure columns 102, 202, impure nitrogen 110, 210 is withdrawn and fed as residual gas through a respective subcooling countercurrent 123, 223 and via the common line 32 to the main heat exchanger 308.
  • an oxygen-enriched bottoms liquid stream 151, 251 is withdrawn and cooled in the respective subcooling countercurrent 123, 223.
  • a first part 153, 253 of the cooled bottom liquid is fed directly to the low-pressure column 102; a second part 154, 254 is introduced into the evaporation space of the top condenser 155, 255 per an argon discharge column 152, 252.
  • the fraction 156 evaporated in the top condenser 155, 255 and the liquid remaining 157 are fed via separate lines into the low-pressure columns 102, 202.
  • the liquid or supercritical air 311 from the main heat exchanger is supplied via lines 111, 211 and 128, 228 in the low pressure columns 102, 202.
  • liquid oxygen 141, 241 is withdrawn from the evaporation spaces of the main condensers 103, 203, combined and fed via line 14 at least partially to an internal compression.
  • the liquid oxygen 14 is pumped by a pump 15 to a high product pressure, evaporated under this high product pressure in the main heat exchanger 308 or (if its pressure is supercritical) pseudo-evaporated, heated to about ambient temperature and finally withdrawn as gaseous pressure oxygen product GOXIC.
  • pressurized nitrogen is withdrawn directly from the head of the high-pressure columns 101, 201 (lines 104, 142 and 204, 242), together via line 42 to the main heat exchanger 308, where it is heated and finally recovered as gaseous compressed nitrogen product MPGAN.
  • a portion 143, 243 of the liquid nitrogen produced in the main condensers 103, 104 is respectively supplied via line 43 to an internal compression (pump 16) and recovered as gaseous high-pressure nitrogen product GANIC.
  • the plant can also supply liquid products LOX, LIN. These can be removed separately from each distillation column system as shown.
  • both low-pressure columns 10, 103 are connected to their respective argon discharge column 152, 252 and their top condenser 155, 255 as in the case of a classic argon recovery.
  • the line pairs 113, 213 are connected to the lower area of an argon discharge column.
  • the internal structure and mode of operation of such a classic argon recovery are, for example, in DE 2325422 A .
  • EP 942246 A2 EP 1103772 A1 .
  • the argon discharge column does not serve to supply an argon product, but to remove argon to improve the oxygen yield.
  • Its "product” consists of the gaseous argon-enriched stream 163, 263 remaining in the argon discharge column top condenser during liquefaction, which is passed via line 164 to a separate passage group of the main heat exchanger 308.
  • the Argonausschleußäulen are housed after the construction of the system in a common cold box with one or two double columns.
  • the mass transfer elements in the two low-pressure columns 102, 202 are formed exclusively by ordered packing.
  • the oxygen sections of the two low-pressure columns 102, 202 are of an ordered packing with a specific packing Surface of 750 m 2 / m 3 or alternatively 1200 m 2 / m 3 equipped, in the remaining sections, the package has a specific surface area of 750 or 500 m 2 / m 3 .
  • the two low pressure columns 102, 202 may have a nitrogen section above the mass transfer sections shown in the drawing; this can then also be equipped with a particularly dense packing (for example with a specific surface area of 1200 m 2 / m 3 for the purpose of reducing the height of the column). By way of derogation, it is possible to combine ordered packing of different specific surface area within each of said sections.
  • the argon discharge columns contained in the 152, 252 included in the embodiment only pack with a specific surface area of 1200 m 2 / m 3 or alternatively 750 m 2 / m 3 .
  • the mass transfer elements are formed exclusively by ordered packing with a specific surface area of 1200 m 2 / m 3 or 750 m 2 / m 3 .
  • at least a portion of the mass transfer elements could be formed in one or both high pressure columns 101, 201 by conventional distillation trays, for example through sieve trays.
  • a multi-stranded system can be made by two or more plants according to FIG. 1 be formed.
  • FIG. 2 there are four strands (trains) Tr1 to Tr4.
  • Each double distillation column system 300 is enclosed by its own cold box 301.
  • all four air separation strands are constructed identically; alternatively, individual or all strands could be designed differently.
  • Each strand comprises an atmospheric air inlet filter 302, a main air compressor 303, an air pre-cooling unit 304, an air purification unit 305 (typically formed by a pair of molecular sieve adsorbers), a Booster Air Compressor 306 with aftercooler 307, and an air condenser 306 Main heat exchanger 308 in its own coldbox 309; These devices are each independent of the other strands.
  • the air recompressed in the reboiler 306 is liquefied in the main heat exchanger 308 (or, if its pressure is supercritical, pseudo-liquefied) and fed via line 311 to the distillation column systems in the cold box 301 where it flows into the streams 111 and 112 of FIG FIG.
  • the warm part (air compression, pre-cooling and air purification) and / or the main heat exchanger may have a different number of strands than the distillation column systems.
  • one distillation column system strand could be supplied by two main air compressor strands or two distillation column system strands from four main air compressor strands.
  • the concept of the invention can also be applied to a process without air recompression 306/307 (for example, with the total air compressed to more than 5 bar above the highest of the operating pressures of the two high pressure columns) or to processes with other elements such as a nitrogen cycle.
  • any known type of turbine circuit can be selected with one, two or more turbines.
  • the double column distillation column systems and the argon discharge column n are in FIG. 2 shown very schematically. It looks in detail like in FIG. 1 described.
  • the number of strands (installations) can be reduced by the invention, in two specific applications from six to five or from five to four.

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  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP14004443.9A 2014-12-30 2014-12-30 Système de colonne de distillation et installation pour la production d'oxygène par séparation cryogénique de l'air Withdrawn EP3040665A1 (fr)

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Cited By (1)

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