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EP3163237A1 - Systeme de colonnes de distillation et procede de production d'oxygene par separation cryogenique de l'air - Google Patents

Systeme de colonnes de distillation et procede de production d'oxygene par separation cryogenique de l'air Download PDF

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Publication number
EP3163237A1
EP3163237A1 EP15003096.3A EP15003096A EP3163237A1 EP 3163237 A1 EP3163237 A1 EP 3163237A1 EP 15003096 A EP15003096 A EP 15003096A EP 3163237 A1 EP3163237 A1 EP 3163237A1
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EP
European Patent Office
Prior art keywords
column
pressure column
air
low
condenser
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Withdrawn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
EP15003096.3A
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German (de)
English (en)
Inventor
Anton Moll
Dimitri Goloubev
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Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP15003096.3A priority Critical patent/EP3163237A1/fr
Publication of EP3163237A1 publication Critical patent/EP3163237A1/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Withdrawn legal-status Critical Current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
    • F25J3/04006—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
    • F25J3/04006—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—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
    • F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
    • F25J3/04448—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system in a double column flowsheet with an intermediate 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
    • F25J3/04642—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
    • F25J3/04763—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
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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
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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
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
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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
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    • 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
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    • 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
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    • 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

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.
  • condenser-evaporator refers to 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, which consist of liquefaction passages or evaporation passages. In the liquefaction space, the condensation (liquefaction) of the first fluid flow is performed, in the evaporation space the evaporation of the second fluid flow. Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • a "main heat exchanger” serves to cool feed air in indirect heat exchange with recycle streams from the distillation column system. It may be formed from a single or multiple parallel and / or serially connected heat exchanger sections, for example 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.
  • top, bottom, “above”, “below”, “above”, “below”, “next to each other", “vertically”, “horizontally” etc. refer here to the spatial orientation of the separation columns in normal operation.
  • An arrangement of two columns or pieces of equipment “one above the other” is understood here to mean that the upper end of the lower of the two apparatus parts is at a lower or the same geodetic height as the lower end of the upper of the two apparatus parts and the projections of the two apparatus parts into one overlap horizontal plane.
  • the two parts of the apparatus are arranged exactly one above the other, that is, the axes of the two columns extend on the same vertical line.
  • a plant of the type mentioned and a corresponding method are made DE 1136355 B known.
  • the invention has for its object to provide such a system very energy efficient and with a particularly high capacity for oxygen production at the same time form so compact that they can be prefabricated as far as possible and then transported to the site.
  • transports there are strict limitations regarding the height (transport length) and the diameter (Transport width) of the separation columns. For example, column diameters of a maximum of 4.8 m are often specified.
  • argon discharge column here refers to a separation column for argon-oxygen separation, which is not used for obtaining a pure argon product but for discharging argon of the air to be separated into the high-pressure column and low-pressure column.
  • Their circuit differs only slightly from that of a conventional crude argon column, but it contains significantly less theoretical plates, namely less than 40, especially between 15 and 30.
  • the bottom portion of an argon discharge column is connected to an intermediate point of the low pressure column and the argon discharge column becomes cooled by a top condenser on the evaporation side relaxed bottom liquid is introduced from the high pressure column; an argon discharge column has no bottom evaporator.
  • auxiliary column a part of the feed air is treated, in particular at least part of a turbine-relaxed air flow, which is conducted neither into the high-pressure column nor into the low-pressure column.
  • the auxiliary column is installed so to speak in the Argonausschleusklale, thereby the height of a column can be saved in the invention or conversely, the throughput in the column at existing height can be increased without the column diameter exceeds the permissible transport dimensions.
  • the combination of ArgonausschleusTalkle and auxiliary column is here as referred to as "common container”.
  • This has in its interior a vertical partition. This can basically have any shape, such as cylindrical shape; Preferably, however, a flat partition wall is used.
  • the two subspaces, which are formed by the partition may be the same or different sizes.
  • the Argonausschleusklan Located on one side of the partition are the Argonausschleusklan, in particular their mass transfer elements, on the other the auxiliary column, in particular their mass transfer elements.
  • the mass transfer processes on both sides of the partition are independent of each other.
  • the argon discharge column overhead condenser can be arranged at the top of the common container. Its liquefaction room here communicates fluidically only with the head of the argon discharge column, but not with the head of the auxiliary column.
  • a first gaseous nitrogen product is obtained, at the top of the low-pressure column a second gaseous nitrogen product.
  • these two nitrogen products may be combined and heated together to about ambient temperature in a supercooling countercurrent and a main heat exchanger.
  • the head of the low-pressure column can be operated under particularly low pressure of, for example, 1.0 to 1.6 bar, wherein at the top of the auxiliary column a pressure of about 0.1 to 0.3 bar higher pressure of 1.1 to 1, 7 bar, which is sufficient to use the top gas of the first gaseous overhead fraction from the auxiliary column as a regeneration gas for a molecular sieve for air purification.
  • the particularly low low-pressure column pressure reduces the energy consumption of the system.
  • the method according to the invention is particularly well suited for systems of particularly high oxygen capacity of, for example, 80,000 to 170,000 Nm 3 / h.
  • These and other capacity figures in the text refer to a maximum column diameter of 4.8 m.
  • the means for introducing a gaseous fraction whose oxygen content is equal to or higher than that of the air are formed in the auxiliary column as means for introducing turbine-relaxed air into the auxiliary column.
  • the turbine air must only be partially introduced into the low-pressure column.
  • the two subspaces of the common container could communicate at their lower end, as is common practice in dividing wall columns.
  • the two subspaces are preferably completely separated from each other by the common container and the partition are formed so that the partition completely seals the two subspaces of the common container against each other.
  • the swamps of argon discharge column and auxiliary column are completely independent of each other, both in chemical composition and in the filling level.
  • High-pressure column, main condenser and low pressure column here form a classic double column.
  • argon discharge column and auxiliary column Such a configuration has a particularly low footprint.
  • This embodiment of the invention has, for example, a capacity of 70,000 to 85,000 Nm 3 / h of oxygen.
  • a "large oxygen capacity” refers to a plant with an oxygen production of more than 140,000 Nm 3 / h, for example up to 170,000 Nm 3 / h and more.
  • the invention also relates to a method for producing oxygen by cryogenic separation of air according to claims 8 to 14.
  • FIG. 1a is to see a plant with a single distillation column system.
  • it has a "mean oxygen capacity" of, for example, 100,000 to 140,000 Nm 3 / h.
  • the distillation column system of the embodiment of the FIG. 1a comprises a high-pressure column 101, a low-pressure column 102, a main condenser 103, an argon discharge column 152 and an auxiliary column 140.
  • the main capacitor 103 is formed in the example by a six-stage cascade evaporator, so a multi-level pocket evaporator.
  • the pair of columns 101/102 is not arranged in the form of a double column, but next to each other.
  • the argon discharge column 152 and the auxiliary column are housed according to the invention in a common container 160 with a vertical partition wall 161.
  • the partition wall 161 is flat in the example and extends from the lid to the bottom of the container, so that the two subspaces forming the argon discharge column 152 and the auxiliary column 140 are completely separated; For example, different levels can also form in the sump, as shown in the drawing.
  • An argon discharge head condenser 155 is located immediately above the common container 160; he is here designed as a single-storey bath evaporator.
  • a shown system comprises an inlet filter 302 for atmospheric air (AIR), a main air compressor 303, an air pre-cooling unit 304, an air cleaning unit 305 (usually formed by a pair of molecular sieve adsorbers), an air compressor 306 (Booster Air Compressor - BAC) with intermediate and aftercoolers and a main heat exchanger 308 on.
  • AIR atmospheric air
  • main air compressor 303 for atmospheric air
  • air pre-cooling unit 304 usually formed by a pair of molecular sieve adsorbers
  • an air compressor 306 Booster Air Compressor - BAC
  • a total compressed air flow 100 from the cold end of the main heat exchanger 308 is introduced into the high pressure column 101.
  • 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 lines 311/111 to the distillation column system.
  • a nitrogen gas stream 104, 114 from the high-pressure column 101 is introduced into the liquefaction space of the main condenser 103. There, liquid nitrogen 115 is generated therefrom, which is passed to the high-pressure column 101 at least to a first part as a first liquid nitrogen stream 105.
  • a liquid oxygen stream 106 from the bottom of the low-pressure column 102 is conveyed to at least part 106 by means of a pump 106a into the evaporation space of the main condenser 103.
  • Gaseous oxygen 106c formed in the evaporation space of the main condenser 103 is introduced into the first low-pressure column 102 where it forms the rising vapor.
  • a second part can be obtained directly as a gaseous oxygen product and heated in the main heat exchanger 308 (not realized in this embodiment).
  • a portion 106d of the liquid oxygen from the pump 106a may be cooled in a subcooling countercurrent 123 and subsequently recovered as a liquid product (LOX).
  • the reflux liquid 109a for the low pressure column 102 is formed by a nitrogen-enriched liquid 120 which is withdrawn at the high pressure column 101 from an intermediate point (or alternatively directly from the top) and cooled in the subcooling countercurrent 123. From the top of the low-pressure column 102, impure nitrogen 110a is withdrawn and passed as residual gas through the supercooling countercurrent 123 and via the line 32 to the main heat exchanger 308. Another part 109b of the nitrogen-enriched liquid 120 from the high-pressure column 101 is fed to the top of the auxiliary column 140. From the top of the auxiliary column 140 also impure nitrogen 110b is withdrawn and mixed with the impure nitrogen 110a from the low pressure column. The bottom liquid 159 of the auxiliary column 140 is guided to the intermediate point of the low-pressure column 102, at which the bottoms liquid 154a of the high-pressure column 101 is also fed.
  • an oxygen-enriched bottoms liquid stream 151 is withdrawn and cooled in the subcooling countercurrent 123.
  • a first part 154a of the cooled bottom liquid 153 is supplied to the low-pressure column 102.
  • the remainder 154b of the cooled bottom liquid 153 is introduced into the evaporation space of the argon discharge head top condenser 155.
  • the vaporized in the top condenser 155 portion 156 and the remaining liquid portion 157 are the low-pressure column 102 fed.
  • the argon-enriched "product" 163 of the argon column is withdrawn in gaseous form from the argon column 152 or its overhead condenser 155 and passed through the main heat exchanger 308 through a separate passage group via line 164.
  • the bottom liquid 158b of the argon discharge column 152 is led to the intermediate point of the low-pressure column 102, on which the gaseous insert 158a for the argon discharge column 152 is withdrawn.
  • the argon-enriched fraction 163 could be mixed with the impure nitrogen 110 and the mixture passed through the main heat exchanger.
  • the liquid air 311 from the main heat exchanger is fed via the line 111 to the high-pressure column 101 at an intermediate point. At least one part 127 is removed again immediately and introduced through the subcooler 123 and via the line 128 into the low-pressure column 102, above the feed of the sump fraction 153. Via line 129 is further gaseous air from a Einblaseturbine 137 in the auxiliary column 140 (line 129a) and / or introduced into the low-pressure column 102 (line 129b). The feed into the low-pressure column takes place at the same point as the feed of the crude oxygen 154a. In a first variant of the embodiment, the entire air 129 is introduced from the injection turbine 137 in the auxiliary column 140. Deviating from this, in a second variant, the air 129 is divided between the two lines 129a and 129b.
  • liquid oxygen 141 is withdrawn from the bottom of the low pressure column 102 and fed via line 14 at least partially to an internal compression.
  • the liquid oxygen 14 is brought by means of 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, warmed to about ambient temperature and finally stripped off as gaseous pressure oxygen product GOXIC.
  • pressurized nitrogen is withdrawn directly from the top of the high-pressure column 101 (lines 104, 142), passed via line 42 to the main heat exchanger 308, warmed there and finally recovered as gaseous pressure nitrogen product MPGAN. Part of it can be used as sealing gas (seal gas).
  • a portion 143 of the liquid nitrogen produced in the main condenser 103 may be 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.
  • the system of FIG. 1a is designed as a two-turbine method with a medium-pressure turbine 138 and an injection turbine 137.
  • FIG. 1b is different from this FIG. 1a that in FIG. 1b only one injection turbine 137, but no intermediate-pressure turbine is provided.
  • FIG. 1 a rejects the system of Figure 1c in the auxiliary column two mass transfer sections 140a and 140b. Between these two sections, a portion 128b of the liquid air 128 is introduced into the auxiliary column.
  • the use of an additional (third) packing section (in Figure 1c not shown) in the auxiliary column below 140b and 129a is possible in principle; then a portion of the gas stream 156 is introduced from the argon overhead condenser at the bottom of the auxiliary column.
  • FIG. 2 is a plant with two distillation column systems (twin columns) shown, which is formed according to the invention. It has a "large oxygen capacity" with an oxygen production of, for example, 140,000 to 170,000 Nm 3 / h.
  • the first distillation column system of the embodiment of the FIG. 2 has a first high-pressure column 101, a first low-pressure column 102, a first main capacitor 103, a first auxiliary column 140 and a first Argonausschleusklale 152 on.
  • a second high-pressure column 201, a second low-pressure column 202, a second main condenser 203, a second auxiliary column 240 and a second argon column 252 belong to the second distillation column system of FIG FIG. 2 illustrated plant.
  • the argon discharge column 152/262 and the auxiliary column 140/240 are each arranged in a common container 160/260 with partition wall 161/261. Both distillation column systems are constructed identically.
  • Both main capacitors 103, 203 are formed in the example by a three-stage cascade evaporator.
  • the pairs of columns 101/102, 201/202 are arranged in the form of two double columns.
  • the common container 160/260 are each arranged above the double columns, so that one can speak of triple columns.
  • the argon column head condensers 155, 255 sit directly above the common containers 140/240 and are designed as a bath evaporator.
  • 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 introduced into the first high-pressure column 101, the second compressed air sub-stream 200 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 211.
  • the argon-enriched "product" 163, 263 of the argon column is removed in gaseous form from the argon discharge column 152, 252 or its top condenser 155, 255 and passed via line 164 through a separate passage group through the main heat exchanger 308.
  • the argon-enriched fractions 163, 263 could be mixed with the impure nitrogen 110a, 110b, 210a, 201b, 32 and the mixture passed through the main heat exchanger.
  • 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, vaporized under this high product pressure in the main heat exchanger 308 or (if its pressure is supercritical) pseudo-evaporated, warmed 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 142 and 242), together via line 42 to the main heat exchanger 308, where it is warmed up and finally recovered as gaseous compressed nitrogen product MPGAN.
  • Part of it can be used as sealing gas (seal gas).
  • sealing gas sealing gas
  • a part 143, 243 of the liquid nitrogen produced in the main condensers 103, 203 can be supplied via line 43 to an internal compression (pump 16) and can be obtained 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.
  • 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 provided with an ordered packing having a specific surface area of 750 m 2 / m 3 or alternatively 1200 m 2 / m 3 , in the remaining sections the packing has a specific surface area of 750 or 500 m 2 / m 3 on.
  • the two low pressure columns 102, 202 may have a nitrogen section above the mass transfer areas 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).
  • the argon columns 152, 252 contain in the exemplary embodiment exclusively pack with a specific Surface of 1200 m 2 / m 3 or alternatively 750 m 2 / m 3 , as well as the auxiliary columns 140 and 240.
  • the mass transfer elements are preferably formed by ordered packing with a specific surface area of 1200 m 2 / m 3 or 750 m 2 / m 3 .
  • 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.
  • FIG. 2 is analogous to FIG. 1a is formed as a two-turbine method with a medium-pressure turbine 138 and an injection turbine 137.
  • a medium-pressure turbine 138 and an injection turbine 137.
  • only one injection turbine can be used (see FIG. 1c) ,
  • 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 plant of FIG. 3 shows how FIG. 1 a only a single distillation column system on.
  • the high-pressure column 101, the main condenser 103 and the low-pressure column 102 are arranged one above the other in the form of a classic double column.
  • the common container 160 with partition 161, auxiliary column 140 and argon discharge column 152 is disposed adjacent to the low-pressure column 102 at a height that allows the bottom liquids 159, 158b of these columns to be introduced into the low-pressure column 102 without pumps.
  • the common container can either be arranged on a scaffold or laterally connected to the low-pressure column 102 or its cold box. An oxygen transfer pump can be omitted since the columns are arranged one above the other.

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  • Engineering & Computer Science (AREA)
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  • Mechanical Engineering (AREA)
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  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP15003096.3A 2015-10-29 2015-10-29 Systeme de colonnes de distillation et procede de production d'oxygene par separation cryogenique de l'air Withdrawn EP3163237A1 (fr)

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1136355B (de) 1961-01-26 1962-09-13 Linde S Eismaschinen Ag Zweign Verfahren und Einrichtung zur Tieftemperaturrektifikation von Gasgemischen
US5836174A (en) * 1997-05-30 1998-11-17 Praxair Technology, Inc. Cryogenic rectification system for producing multi-purity oxygen
US20020178747A1 (en) * 2001-03-21 2002-12-05 Linde Aktiengesellschaft Obtaining argon using a three-column system for the fractionation of air and a crude argon column
US6748763B2 (en) 2000-05-31 2004-06-15 Linde Ag Multistoreyed bath condenser
EP2161063A1 (fr) * 2008-09-03 2010-03-10 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Méthode de construction d'une colonne avec partition
FR2964451A3 (fr) * 2011-12-05 2012-03-09 Air Liquide Installation de separation d'un gaz de l'air par separation cryogenique
EP2865978A1 (fr) 2013-10-25 2015-04-29 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air à basse température

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1136355B (de) 1961-01-26 1962-09-13 Linde S Eismaschinen Ag Zweign Verfahren und Einrichtung zur Tieftemperaturrektifikation von Gasgemischen
US5836174A (en) * 1997-05-30 1998-11-17 Praxair Technology, Inc. Cryogenic rectification system for producing multi-purity oxygen
US6748763B2 (en) 2000-05-31 2004-06-15 Linde Ag Multistoreyed bath condenser
EP1287302B1 (fr) 2000-05-31 2005-09-21 Linde AG Condenseur a bain a plusieurs etages
US20020178747A1 (en) * 2001-03-21 2002-12-05 Linde Aktiengesellschaft Obtaining argon using a three-column system for the fractionation of air and a crude argon column
EP2161063A1 (fr) * 2008-09-03 2010-03-10 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Méthode de construction d'une colonne avec partition
FR2964451A3 (fr) * 2011-12-05 2012-03-09 Air Liquide Installation de separation d'un gaz de l'air par separation cryogenique
EP2865978A1 (fr) 2013-10-25 2015-04-29 Linde Aktiengesellschaft Procédé de décomposition à basse température de l'air et installation de décomposition de l'air à basse température

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
HAUSEN; LINDE: "Tieftemperaturtechnik", 1985
LATIMER, CHEMICAL ENGINEERING PROGRESS, vol. 63, no. 2, 1967, pages 35

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