EP3067648A1 - Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air - Google Patents

Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air Download PDF

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Publication number
EP3067648A1
EP3067648A1 EP15000744.1A EP15000744A EP3067648A1 EP 3067648 A1 EP3067648 A1 EP 3067648A1 EP 15000744 A EP15000744 A EP 15000744A EP 3067648 A1 EP3067648 A1 EP 3067648A1
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Prior art keywords
column
pressure column
condenser
argon
low
Prior art date
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EP15000744.1A
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German (de)
English (en)
Inventor
Anton Moll
Stefan Lochner
Ayhan Yayli
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Linde GmbH
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Linde GmbH
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Priority to EP15000744.1A priority Critical patent/EP3067648A1/fr
Publication of EP3067648A1 publication Critical patent/EP3067648A1/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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
    • F25J3/04406—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
    • F25J3/04642—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
    • 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
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • 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
    • F25J3/04933—Partitioning walls or sheets
    • F25J3/04939—Vertical, e.g. dividing wall columns
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/32—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/58—One fluid 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.
  • an "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 region of an argon discharge column is connected to an intermediate point of the low pressure column and the argon discharge column is passed through cooled a top condenser, on the evaporation side relaxed bottom liquid from the high pressure column or another cooling liquid is introduced; an argon discharge column has no bottom evaporator.
  • the main condenser and the argon discharge head condenser are designed in the invention as a condenser-evaporator.
  • the term "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.
  • 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 prefabricated systems.
  • 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 parts of equipment “one above the other” is understood here that the upper end of the lower of the two parts of the apparatus is in working condition at lower or same geodetic height as the lower end of the upper of the two parts of the apparatus and the projections of the two parts of the apparatus overlap in a 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.
  • “Side by side” two apparatuses stand if their projections do not overlap in a horizontal plane; The two apparatuses are then regularly arranged at least partially at the same height.
  • a distillation column system of the type mentioned is out US 5235816 known. Such systems are prefabricated regularly as far as possible in the production, the prefabricated parts are transported to the site and finally connected there. Depending on the size of the system, for example, the entire double column can be transported with its coldbox. If the size of the system no longer allows this, the double column - possibly in two or more parts - is transported without a coldbox. An additional column such as the argon discharge column causes additional effort with its own cold box, which must be brought separately to the construction site regularly and mounted on an elaborate frame.
  • 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, especially for particularly large air separation plants for an air volume of more than 370,000 Nm 3 / h, preferably more than 1,000,000 Nm 3 / h.
  • An arrangement of two columns "next to each other" means that the two columns are positioned in the operational state of the plant so that the projections of their cross sections do not overlap on a horizontal plane. Frequently, the lower ends of the two columns are at about the same geodetic height plus / minus 5 m.
  • the transport length of the low-pressure column is also higher due to the incorporation of the argon discharge column according to the invention into a dividing-wall column section of the low-pressure column.
  • the main condenser is disposed between the high pressure column and the argon discharge column overhead condenser. This results in a total of a particularly compact arrangement.
  • main condenser and argon discharge column overhead condenser are arranged in a common first cold box.
  • no further capacitors or heat exchangers, such as subcooling countercurrents, are accommodated in the first coldbox.
  • the low-pressure column can be accommodated in a separate second coldbox. In many cases, however, it is better to arrange the low-pressure column also in the first cold box.
  • the cross-section of the two compartment forming the argon discharge column is 25 to 60%, preferably between 30% and 50%, of the total cross section of the middle section of the low pressure column.
  • the distillation column system further comprises an auxiliary column whose sump region is designed to introduce a portion of the gas from the vaporization space of the argon discharge head condenser, and also to provide a liquid nitrogen line for introducing liquid nitrogen to the overhead of the auxiliary column.
  • auxiliary column whose sump region is designed to introduce a portion of the gas from the vaporization space of the argon discharge head condenser, and also to provide a liquid nitrogen line for introducing liquid nitrogen to the overhead of the auxiliary column.
  • 20 to 100% of the gas generated in the evaporation space of the argon discharge head condenser is introduced into the auxiliary column.
  • the remainder if present, can be introduced into the low-pressure column.
  • One or more liquid lines for one or more liquids lead from one or more intermediate points or the bottom of the auxiliary column in the low-pressure column. This return liquid and / or bottom liquid of the auxiliary column is introduced as an additional intermediate return to the low pressure column.
  • an intermediate fraction of the high-pressure column can be introduced into the auxiliary column via an intermediate fraction line.
  • any fraction that would otherwise go into the low-pressure column, the separation in the auxiliary column are fed, for example, a turbine air flow.
  • the intermediate fraction can be formed for example by liquid air.
  • the distillation column system has means for collecting at least part of the liquid flowing down in the auxiliary column and means for introducing the collected liquid into the low-pressure column.
  • the effluent from the auxiliary column liquid is not mixed with the bottoms liquid and can be at least partially fed into the low-pressure column and that separated from the bottoms liquid from the evaporation space of the argon discharge head condenser.
  • the invention also relates to a method for the production of oxygen by cryogenic separation of air according to claim 10. This method can be supplemented analogously by further features of all dependent device claims.
  • the distillation column system of the embodiment of the FIG. 1 has a high pressure column 1, a low pressure column 2 and a main capacitor 3.
  • the main capacitor 3 is designed here as a multi-storey bath evaporator, more precisely as a cascade evaporator.
  • the high pressure column 1 and the low pressure column 2 are arranged side by side; in particular, their lower ends are at a similar geodesic level.
  • the low-pressure column 2 may be set up slightly higher than the high-pressure column 1.
  • the low-pressure column 2 has a lower portion A1, a middle portion A2 and an upper portion A3.
  • a first partial stream 4 of the feed air flows in gaseous form into the high-pressure column 1, specifically directly above the sump.
  • a second part 5 of the feed air is at least partially liquid and is fed to the high-pressure column 1 at an intermediate point. At least a portion of the liquid air is taken out again via line 6, cooled in a subcooling countercurrent 7 and fed via line 8 of the low pressure column 2 at a first intermediate point, which lies in an intermediate region of the upper section A3.
  • a part 10 of the gaseous top nitrogen 9 of the high-pressure column 1 is at least partially condensed.
  • the liquid nitrogen 11 obtained in the process is fed to a first part 12 as reflux to the top of the high-pressure column 1.
  • a second part 13 is supplied to an internal compression (not shown) and finally recovered as gaseous pressure nitrogen product.
  • Another part 14 of the gaseous head nitrogen 9 is warmed up in the main heat exchanger (not shown) and recovered directly as a gaseous pressure product.
  • Liquid raw oxygen 15 from the high-pressure column 1 is cooled in the subcooling countercurrent 7 and via the line 16 to a argon discharge column head capacitor 17 and further via the lines and 18/19 of the low pressure column. 2 fed at a second intermediate point, which is below the first intermediate point, at the lower edge of the upper portion A3.
  • Liquid impurity nitrogen 35 is withdrawn from an intermediate point of the high-pressure column 1, cooled in the subcooling countercurrent and fed via line 36 to the top of the low-pressure column 2. Part of this can be recovered via line 37 as a liquid nitrogen product (LIN). From the top of the low-pressure column 2 gaseous impurity nitrogen 38 is withdrawn and passed after heating in the subcooling countercurrent 7 via line 39 on to the main heat exchanger (not shown).
  • LIN liquid nitrogen product
  • Liquid oxygen 20 from the bottom of the low-pressure column 2 is conveyed to a first part 22 by means of a pump 21 into the evaporation space of the main condenser 3 and there at least partially evaporated. Resulting gas 23 is returned to the bottom of the low-pressure column 2, where it serves as an ascending gas.
  • a second portion 24 of the liquid oxygen 20 is cooled in the subcooling countercurrent 7 and withdrawn via line 25 as a liquid oxygen product (LOX).
  • a fourth portion 26 of the liquid oxygen 20 is fed to an internal compression (not shown) and finally recovered as a gaseous pressure oxygen product which is the major product of the distillation column system.
  • the middle section A2 of the low-pressure column 2 is formed as a partition wall section.
  • a vertical partition wall 27 separates a first subspace 28 and a second subspace 29 from each other.
  • the partition wall 27 is formed in the example by a flat sheet, which is welded on both sides with the column wall. Both subspaces contain mass transfer elements, for example ordered packing. The mass transfer layers in the subspaces may or may not be the same.
  • the two subspaces can be the same or different sizes.
  • the first subspace 28 forms the argon portion of the low pressure column 2. It communicates at the bottom with the lower portion A1 and at the top with the upper portion A3 in fluid communication. As a result, a first part of the gas can flow from the lower section A1 through the first subspace 28 to the upper section A3. Conversely, liquid flows from the upper section A3 through the first compartment 28 into the lower section A1.
  • the second subspace 29 forms an argon discharge column 31. It is also connected to the lower section A1 in fluid communication below, so that from there a second part of the gas rising from the first section A1 can flow. Above, however, it is gas-tightly sealed with a horizontal wall 30 opposite the upper section A3.
  • the horizontal wall is approximately semicircular and welded to the column wall and the partition wall 27. Neither gas can flow from the head of the argon discharge column 31 into the upper section A3, nor liquid from there can penetrate into the argon discharge column 31.
  • Argon-enriched gas 32 is withdrawn from the top of the argon discharge column 31 and partially liquefied in the liquefaction space of the argon discharge column top condenser 17.
  • the generated liquid 33 is returned as reflux into the Argonausschleusklale 31.
  • the gaseous remaining fraction is removed as argon-enriched "product" 34 in gaseous form from the argon discharge column top condenser 17 and passed as residual gas through a separate passage group of the main heat exchanger (not shown).
  • the argon discharge columns 31 By integrating the argon discharge columns 31 into the low-pressure column 2 and by arranging the argon discharge column overhead condenser above the high-pressure column 1, the argon discharge consumes no additional set-up area compared to the pure nitrogen-oxygen separation.
  • the column diameters are limited for transport height reasons.
  • the diameter of the low-pressure column 2 is below and above the partition wall section maximum in terms of this limitation. The increase in the oxygen yield and the efficiency of the separation can thus be achieved without significant increase in the plant.
  • a packing of higher density than in the first partial space 28 is used in the second partial space 29 (argon discharge column 31), for example 750 m 2 / m 3 parallel to 500 m 2 / m 3 or 500 m 2 / m 3 parallel to 350 m 2 / m 3 .
  • the entire rising from the section A1 gas can be passed through the first compartment 28, without flooding cause the low pressure column 2.
  • the packing in the first compartment 28 should therefore be less dense than that in the oxygen section A1.
  • FIG. 2 is different from the one of FIG. 1 by an auxiliary column 140 and by the introduction of turbine-relaxed air 141 in the low pressure column 2.
  • auxiliary column 140 and by the introduction of turbine-relaxed air 141 in the low pressure column 2.
  • the turbine-relaxed air 141 could alternatively be introduced into the auxiliary column 140 or distributed into the auxiliary column 140 and the low-pressure column 2.
  • the described features for dealing with turbine-relaxed air can also in the embodiment of the FIG. 1 be applied.
  • the auxiliary column 140 and the argon discharge column head condenser 17 are arranged in a common container in such a way that the argon discharge head condenser 17 acts as a sump heater of the auxiliary column 140.
  • the gas from the evaporation chamber of the argon discharge column head condenser 17 is not introduced into the low-pressure column (line 18 in FIG. 1 ), but introduced as ascending gas in the auxiliary column 140.
  • a portion 108b of the supercooled liquid air 108 may be supplied to the auxiliary column 140 at an intermediate location.
  • the rest of 108a goes as in FIG. 1
  • gaseous impure nitrogen 138b is withdrawn and mixed with the gaseous impure nitrogen 138a from the top of the low-pressure column 2.
  • the total flow 38 is passed after heating in the subcooling countercurrent 7 via line 39 on to the main heat exchanger (not shown).
  • the two nitrogen streams 138a, 138b may also be passed separately to and through the main heat exchanger; In this case, the two columns can be operated with different head pressure and thus energy can be saved if necessary.
  • auxiliary column 140 of the upper section A3 of the low-pressure column is relieved.
  • This can therefore be designed with a lower capacity.
  • a less dense packing can be used with constant column diameter and thus the height of the low-pressure column 2 can be reduced.
  • the embodiment of the FIG. 2 a cup 150 in the auxiliary column 140 and a conduit 151.
  • the liquid flowing down in the auxiliary column 140 is partially or completely collected in the cup 150 above the argon discharge column top condenser.
  • the collected liquid is partially or completely introduced via the line 151 in the low pressure column 2, preferably above the line 18. This is a mixture of this liquid with the raw liquid oxygen 16 from the high-pressure column 1 and the non-evaporated liquid from the evaporation space of the argon discharge head condenser 17 avoided.
  • an advantageous control of the argon discharge column head capacitor is possible.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP15000744.1A 2015-03-13 2015-03-13 Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air Withdrawn EP3067648A1 (fr)

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Publication number Priority date Publication date Assignee Title
CN109520207A (zh) * 2017-09-18 2019-03-26 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的方法和单元
CN112469952A (zh) * 2018-08-22 2021-03-09 林德有限责任公司 空气分离设备、用于借助于空气分离设备低温分离空气的方法和用于创建空气分离设备的方法

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DE827364C (de) 1949-04-23 1952-06-13 Linde Eismasch Ag Verfahren zur Gewinnung von Sauerstoff
US2762208A (en) 1952-12-19 1956-09-11 Air Reduction Separation of the constituents of air
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US5235816A (en) 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
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US6748763B2 (en) 2000-05-31 2004-06-15 Linde Ag Multistoreyed bath condenser
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US2762208A (en) 1952-12-19 1956-09-11 Air Reduction Separation of the constituents of air
BE644230A (fr) * 1963-02-25 1964-06-15
US5235816A (en) 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
EP1108965A1 (fr) * 1999-12-13 2001-06-20 Air Products And Chemicals, Inc. Procédé de distillation d'un mélange convenant pour la production d'un courant enrichi en argon dans un procédé cryogénique de séparation de l'air
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
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109520207A (zh) * 2017-09-18 2019-03-26 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的方法和单元
CN109520207B (zh) * 2017-09-18 2022-04-08 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的方法和单元
CN112469952A (zh) * 2018-08-22 2021-03-09 林德有限责任公司 空气分离设备、用于借助于空气分离设备低温分离空气的方法和用于创建空气分离设备的方法
CN112469952B (zh) * 2018-08-22 2022-06-14 林德有限责任公司 空气分离设备、用于借助于空气分离设备低温分离空气的方法和用于创建空气分离设备的方法

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