EP3067649A1 - 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
EP3067649A1
EP3067649A1 EP15000750.8A EP15000750A EP3067649A1 EP 3067649 A1 EP3067649 A1 EP 3067649A1 EP 15000750 A EP15000750 A EP 15000750A EP 3067649 A1 EP3067649 A1 EP 3067649A1
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Prior art keywords
column
oxygen
argon
pressure column
condenser
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EP15000750.8A
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German (de)
English (en)
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Stefan Lochner
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Linde GmbH
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Linde GmbH
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Priority to EP15000750.8A priority Critical patent/EP3067649A1/fr
Priority to DE102016002115.2A priority patent/DE102016002115A1/de
Publication of EP3067649A1 publication Critical patent/EP3067649A1/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Withdrawn legal-status Critical Current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
    • F25J3/04084—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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F25J3/04715—The auxiliary column system simultaneously produces 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
    • F25J3/04763—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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/08—Processes or apparatus using separation by rectification in a triple pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • 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
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface

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.
  • 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, but it contains significantly less theoretical plates, namely less than 40, especially between 35 and 15.
  • 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 head condenser, on the evaporation side relaxed bottom liquid is introduced from the high pressure column; an argon discharge column has no bottom evaporator.
  • argon-oxygen column here refers to an argon-oxygen separation column formed either from a crude argon column having up to 80 theoretical plates or from an argon discharge column which generally produces a less pure overhead product.
  • An argon-oxygen column has no bottom evaporator but an argon-oxygen column top condenser.
  • the main condenser and the argon-oxygen column top condenser are formed 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 a first fluid flow is performed, in the evaporation space the evaporation of a 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 as well as 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 apparatus “one above the other” is understood here to mean that the upper end of the lower of the two apparatus parts is at 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 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 plant no longer allows this, the double column - in one piece or possibly in two or more parts - transported without coldbox.
  • An additional column such as the argon-oxygen column causes additional effort with its own cold box and supporting steel structure. It has to be brought to the construction site separately on a regular basis and there with a relatively large amount of on-site work Rest of the system can be connected. For many plants that need to be transported over long distances by land, maximum transport heights that limit the diameter of the columns apply. In order to realize larger oxygen capacities with limited diameter, one generally uses less and less dense packing. As a result, the separation columns are getting longer or higher.
  • the invention has for its object to make a distillation column system of the type mentioned as compact as possible and in particular to reduce its height while maintaining capacity, especially for very large air separation plants for an air volume of more than 300,000 Nm 3 / h, preferably more than 360,000 Nm 3 / h.
  • the argon-oxygen column is extended downwards by a further mass transfer area, which is used as an oxygen column.
  • This can - like the other sections in high-pressure column, low-pressure column and argon-oxygen column - by conventional rectification soils such as sieve trays, random packing (disordered packing) or ordered (structured) pack are formed.
  • ordered packing is used in the low-pressure column and in the argon-oxygen column.
  • an ascending gas In order to effect a mass transfer, an ascending gas must be introduced below the further mass transfer area. This is done by "means for introducing an oxygen-rich gas" in the bottom of the column of oxygen.
  • the “oxygen-rich gas” can either be introduced from the outside into the oxygen column or originate from a bottom evaporator arranged in the bottom of the oxygen column. When introduced from the outside, the “oxygen-rich gas” is withdrawn at any point of the low-pressure column below the gas outlet, which serves to feed gas into the argon-oxygen column and introduced into the container below the gas feed to the argon-oxygen column. This stream thus has a higher oxygen content than the gas outlet into the argon-oxygen column.
  • This oxygen content is at least 80%, preferably more than 90%, in particular more than 97%.
  • this oxygen content corresponds to the concentration of the oxygen-rich gas in the bottom of the Low pressure column and is withdrawn over the main capacitor.
  • the return, which arrives at the bottom of the column of oxygen, is fed back to the low-pressure column, ideally at the same point where the gas for feeding into the column of oxygen is withdrawn from the low-pressure column.
  • a bottom evaporator can be installed in the bottom of the oxygen column. Basically, you can make the capacity equalization between the oxygen column and the low pressure column with liquid instead of gas from the low pressure column, then gas would flow from the oxygen column back into the low pressure column.
  • the container of the argon-oxygen column is not only used as usual for argon enrichment of the argon-oxygen mixture from the low-pressure column, but also for depletion of the down-flowing liquid to argon and thus for the accumulation of oxygen.
  • the lower part of the container, the oxygen column thus acts much like a corresponding part of the oxygen portion of the low-pressure column and is connected to this practically in parallel.
  • the corresponding part of the oxygen section is relieved, since there flow less gas and liquid during operation of the system.
  • the ratio between the gas quantity rising there and in the oxygen column is from 20:80 to 50:50.
  • the relevant part of the oxygen section can therefore be equipped with a reduced capacity, for example by using a denser packing.
  • this increases the effectiveness of the section and the section can be built lower. In this way, the overall height of the low-pressure column or the entire double column is reduced. Prefabrication, transport and construction of the double column require correspondingly less effort.
  • the oxygen column is preferably formed so that the oxygen concentration in its sump is equal to that in the bottom of the low-pressure column.
  • the "part of the oxygen section” described above is formed by the entire oxygen section between the bottom of the low-pressure column and the gas line to the argon-oxygen column.
  • the means for introducing an oxygen-rich gas through an oxygen gas line for the introduction of oxygen-rich gas from the low pressure column formed in the bottom region of the oxygen column can also have a bottom evaporator in this variant; In general, however, it is carried out in the first variant without sump heating.
  • the load distribution can be shifted via an additional liquid line, which is preferably drawn off at the same point of the low-pressure column as the gas line. In this case, one would return gas from the oxygen column in the low-pressure column in order not to unnecessarily burden the argon-oxygen column.
  • the oxygen column has an oxygen column bottom heating, which is designed as a condenser-evaporator, wherein the evaporation space of the oxygen column bottom heating is in particular in flow connection with the bottom region of the oxygen column.
  • the oxygen column bottom heater is arranged so that the bottoms liquid of the oxygen column can flow into the low pressure column by virtue of the hydrostatic pressure gradient.
  • the distillation column system may further comprise a second high-pressure column which is disposed below the container of the argon-oxygen column and whose head portion is in fluid communication with the liquefaction space of the oxygen column sump heater.
  • the combination of argon-oxygen column and oxygen column (top) and second high-pressure column (bottom) thus form a kind of double column with the oxygen column bottom heater as a "main capacitor”.
  • the capacity distribution between the first and second high-pressure column is for example about 60 to 40.
  • the second high pressure column of the complete first high pressure column can be connected in parallel. In many cases, however, it is more favorable if the bottom region of the second high-pressure column is connected via a nitrogen gas feed line and a liquid nitrogen return line to an intermediate point of the first high-pressure column.
  • the discharge acts specifically for the area of the first high-pressure column above the connection with the nitrogen gas supply line.
  • the warm part of the air separation plant and the main heat exchanger are executed in a usual way and therefore not shown in the drawings.
  • the argon-oxygen column is formed by an argon discharge column and the argon-oxygen column top condenser through an argon discharge column top condenser.
  • the embodiments are basically also suitable for the case that the argon-oxygen column is formed by a crude argon column, that is, has more theoretical plates than an argon discharge column.
  • first feed air stream 1 which was purified of water and carbon dioxide and cooled to about dew point, under a pressure of, for example, 5.5 bara gaseously introduced into a first high-pressure column 2.
  • a second feed air stream 5 is introduced liquid into the first high-pressure column 2; a part 6 of which is immediately removed again, cooled in a supercooling countercurrent 7 and fed via line 7 into the low-pressure column 4.
  • the gaseous head nitrogen 8 of the first high-pressure column is introduced to a part 9 in the liquefaction space of the main condenser 3. Liquid nitrogen 10 produced in this process is cooled to a first part 11 in the subcooling countercurrent 7 and recovered as liquid nitrogen product LIN. The remainder 12 is given up as reflux to the top of the first high-pressure column 2. Via line 13, another part of the gaseous nitrogen head 8 of the first high-pressure column 2 can be obtained as a gaseous pressure product. Impure liquid nitrogen 14 is withdrawn from an intermediate point of the first high pressure column 2, cooled in the subcooling countercurrent 7 and fed via line 15 to the top of the low pressure column 4.
  • oxygen is withdrawn as the main product of the system, namely as liquid oxygen 16 from the bottom of the low-pressure column 4 (or from the evaporation space of the main condenser 3).
  • the liquid oxygen is supplied via line 17 to an internal compression. It is brought to an elevated pressure in the liquid state, evaporated or pseudo-evaporated under this increased pressure in the main heat exchanger (if the increased pressure is supercritical) and finally delivered as a gaseous pressure product (these process steps and the corresponding apparatus parts are not shown here).
  • Another liquid oxygen fraction 41 is withdrawn above the main condenser 3, optionally cooled in the subcooling countercurrent 7 and finally recovered as a liquid oxygen product LOX.
  • gaseous impurity nitrogen 18 is removed as residual gas and passed through the supercooling countercurrent 7 and via line 19 to the cold end of the main heat exchanger.
  • An argon discharge column 26 is disposed in a container 20. Further down in the same container 20 is an oxygen column 36.
  • the container, the argon discharge column 26 and the oxygen column 36 are connected through a gas line 21 and a liquid line 22 to an intermediate point of the low pressure column 4. With the two lines you can adjust the capacity in the oxygen column 36. If the liquid line 22 is closed (or is missing), the capacity between the two columns is distributed in such a way that the conversion in the output (the oxygen column 36) corresponds to the turnover of the lift (the argon discharge column). If more capacity in the output of the container 20 (the oxygen column 36) are moved, is opposite to the in FIG. 1 drawn flow direction - liquid transported from the low pressure column 4 in the oxygen column 36.
  • gas line 21 and liquid line 22 can also be combined in a single line with a particularly large cross-section.
  • the argon discharge column has an argon discharge head condenser 23, the liquefaction space of which communicates with the head of the argon discharge column via lines 24 (gas) and 25 (liquid).
  • the argon discharge column top condenser 23 can - as shown - be realized as a bath evaporator.
  • the evaporation space of the argon discharge column head condenser 23 is in flow communication with the sump of the first high-pressure column.
  • raw liquid oxygen from the sump of the first high-pressure column 2 is introduced via these lines 28, 29, 30. This evaporates partially and is then via a gas line 31 and a liquid line 32 introduced into the low-pressure column 4.
  • the entire amount 29 can be passed through the condenser 23.
  • argon discharge column 26 which contains about 10 mol% of argon and, moreover, mainly consists of oxygen.
  • argon discharge column 26 argon is enriched.
  • line 27 a residual gas leaves the argon discharge column 26 and the argon discharge column top condenser 23, which contains about 75 mol% of argon.
  • Line 27 in turn leads to the cold end of the main heat exchanger, not shown.
  • argon discharge column 26 corresponds to a conventional argon discharge column.
  • the oxygen column 36 which is arranged in the container 20 below the gas line 21 and thus below the argon discharge column 26, is additionally installed in its container 20.
  • the oxygen column 36 has in its sump region means 35 for introducing an oxygen-rich gas.
  • the bottom liquid 34 of the oxygen column 36 has approximately the same composition as the bottoms liquid 16 of the low-pressure column 4 and is mixed with this.
  • the bottom liquid 34 can be wholly or partly fed into the line 41 and recovered as a liquid product LOX (not shown in the drawing).
  • gaseous oxygen 35 is introduced from the bottom region of the low-pressure column 4 or from the evaporation chamber of the main condenser 3 into the bottom region of the oxygen column 36 and serves there as an ascending gas.
  • copper packing 40, 39 are inserted at the bottom.
  • copper here is pure copper or a Alloy having a copper content of at least 67%, preferably at least 80%, most preferably at least 90% understood (in each case based on the mass).
  • the term “copper” includes all materials specified in Annex C of the EIGA document IGC Doc 13/02 / E as “copper” and "copper-nickel alloys"("Copper” / "Copper-Nickel Alloys” in EIGA - OXYGEN PIPELINE SYSTEMS - IGC Doc 13/02 / E issued 10 by the European Industrial Gases Association).
  • the remaining packing layers of the lowermost packing sections 37, 38 of the low pressure column are formed by a conventional ordered aluminum package.
  • the details of using a copper packing in the low pressure column are in EP 2645031 A1 described.
  • the gaseous oxygen generated in the main condenser 3 flow as ascending gas into the lowest mass transfer section 37 of the low-pressure column 4.
  • the remaining 40% pass via line 35 into the oxygen column 36 and form the ascending vapor in the lowest mass transfer section 38 there.
  • the oxygen portion of the low-pressure column 4 (up to the gas supply line 21) is relieved by 40%.
  • a particularly dense packing can be used there and thus height can be saved.
  • the load between the two columns is distributed so that the lowest possible column heights for both columns.
  • a portion 209 of the overhead nitrogen 208 of the second high pressure column 202 is condensed; the remainder 213 can be obtained as a gaseous pressure product and optionally mixed with top nitrogen 13 from the first high-pressure column 2.
  • the direct nitrogen product from the high pressure columns is then fed via a common conduit 113 to the main heat exchanger.
  • the liquid nitrogen 210 recovered in the oxygen column sump heater 203 becomes a first part 212 of the first one High pressure column 2 and a second part 211 of the second high-pressure column 202 as reflux abandoned.
  • the liquid oxygen fractions 16, 34 are combined from the bottoms of the oxygen column 36 and the low-pressure column 4 (17). This can be done either through a common piping or that - diverging from the drawing - the bottom liquid of a column passed into the bottom of the other and from there the common product is withdrawn.
  • the sump of the second high-pressure column 202 is connected to an intermediate point of the first high-pressure column 2 via a gaseous nitrogen supply line 241 and an impure liquid nitrogen liquid return line 242.
  • the main condenser 3 and the uppermost portion of the first high pressure column 2 are relieved in addition to the oxygen portion of the low pressure column 4 by 40% of the ascending in the first high pressure column 2 steam are passed via the gas supply line 241 in the second high pressure column 202. Accordingly, less gas condenses in the main condenser 3; the "missing" amount of liquid nitrogen is generated in the oxygen column sump heater 203. Thus, the height of the main condenser 3 and the uppermost portion (above the gas supply line 241) of the first high-pressure column 2 can be reduced.
  • FIG. 3 shows a modification of the embodiment of FIG. 2 .
  • the downflowing liquid can be further enriched in oxygen, for example to about 20 percent.
  • the sump of the second high-pressure column is connected to a second intermediate point of the first high-pressure column 2, preferably to the point at which the liquid feed air 5 is fed. In this way, in addition, the portion of the first high-pressure column 2 between the lines 242 and 341 is relieved.
  • FIG. 4 includes the second high pressure column 202 opposite FIG. 3 yet another mass transfer section 450 and thus can be operated completely parallel to the first high-pressure column 2.
  • the oxygen-enriched bottom liquid 442 of the second high-pressure column 202 is combined with the bottoms liquid 28 from the first high-pressure column and passed on together via the line 428.
  • Rising gas for the second high-pressure column 202 is formed by a portion 401 of the first gaseous feed air stream 1, which is introduced into the sump area of the second high-pressure column 202.
  • the load of the complete first high pressure column can be optimized by introducing appropriate amounts into the second high pressure column and deducted from it. The height of the first high-pressure column can thus be further reduced.
  • FIG. 5 shows a further modification of the embodiment of FIG. 2 ,
  • a side column 504 is used for low-pressure column 4, wherein the argon discharge column head capacitor 23 acts as bottom evaporator of the side column 504.
  • container 20 with Argonausschleuskla 26 and oxygen column 36 and second high-pressure column 202 - FIG. 5 shown - are arranged one above the other, they result in a triple column.
  • the portion of bottoms liquid not vaporized in the argon discharge head condenser 23 is fed to the low-pressure column 4 at an intermediate point which is above the intermediate point at which the low-pressure column 4 via a gas line 21 and a liquid line 22 for an argon-enriched Fraction is connected to the argon discharge column 26.
  • the two nitrogen streams 18, 518 can also be passed separately to and through the HWT, so that the low-pressure column and the side column can be driven with different head pressures.
  • FIG. 6 shows FIG. 6 a combination of the side column 504 of FIG. 5 with a second high pressure column 202 according to FIG. 4 ; deviating from FIG. 4 here is the second high-pressure column 202 only at the bottom (line 442) and at the top (lines 211 and 213) connected to the first high-pressure column 2.
  • the second high-pressure column 202 here generates only impure nitrogen 208, which can be used in liquid form 211 in the first high-pressure column 2 and / or in the low-pressure column 4 as reflux;
  • a gaseous pressure product 213 of about the same composition in the second high-pressure column 202 is obtained.
  • the second high-pressure column 202 can be significantly shorter and thus cheaper than in FIG. 4 be executed.
  • the column size can be adapted flexibly to the existing boundary conditions.

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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)
EP15000750.8A 2015-03-13 2015-03-13 Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air Withdrawn EP3067649A1 (fr)

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EP15000750.8A EP3067649A1 (fr) 2015-03-13 2015-03-13 Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air
DE102016002115.2A DE102016002115A1 (de) 2015-03-13 2016-02-23 Destillationssäulen-System und Verfahren zur Erzeugung von Sauerstoff durch Tieftemperaturzerlegung von Luft

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EP15000750.8A EP3067649A1 (fr) 2015-03-13 2015-03-13 Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3327393A1 (fr) * 2016-11-25 2018-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de produit d'oxygène ultrapur par cryogénie de séparation d'air
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
WO2022263013A1 (fr) 2021-06-17 2022-12-22 Linde Gmbh Procédé et installation permettant de fournir un produit à base d'air gazeux sous pression riche en oxygène

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EP0299364A2 (fr) * 1987-07-09 1989-01-18 Linde Aktiengesellschaft Procédé et dispositif de séparation de l'air par rectification
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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EP2645031A1 (fr) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Colonne de séparation pour une installation de décomposition de l'air à basse température, installation de décomposition de l'air à basse température et procédé de décomposition à basse température de l'air

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EP0299364A2 (fr) * 1987-07-09 1989-01-18 Linde Aktiengesellschaft Procédé et dispositif de séparation de l'air par rectification
US5235816A (en) 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
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EP1287302B1 (fr) 2000-05-31 2005-09-21 Linde AG Condenseur a bain a plusieurs etages
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EP2645031A1 (fr) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Colonne de séparation pour une installation de décomposition de l'air à basse température, installation de décomposition de l'air à basse température et procédé de décomposition à basse température de l'air

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3327393A1 (fr) * 2016-11-25 2018-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de produit d'oxygène ultrapur par cryogénie de séparation d'air
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
WO2022263013A1 (fr) 2021-06-17 2022-12-22 Linde Gmbh Procédé et installation permettant de fournir un produit à base d'air gazeux sous pression riche en oxygène

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