EP2965029B1 - Luftzerlegungsanlage, verfahren zur gewinnung eines argon enthaltenden produkts und verfahren zur erstellung einer luftzerlegungsanlage - Google Patents

Luftzerlegungsanlage, verfahren zur gewinnung eines argon enthaltenden produkts und verfahren zur erstellung einer luftzerlegungsanlage Download PDF

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EP2965029B1
EP2965029B1 EP14716232.5A EP14716232A EP2965029B1 EP 2965029 B1 EP2965029 B1 EP 2965029B1 EP 14716232 A EP14716232 A EP 14716232A EP 2965029 B1 EP2965029 B1 EP 2965029B1
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Prior art keywords
column
low
pressure column
section
argon
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German (de)
English (en)
French (fr)
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EP2965029A2 (de
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Stefan Lochner
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Linde GmbH
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Linde GmbH
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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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/028—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 characterised by the separated product stream separation of noble gases
    • F25J3/0285—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 characterised by the separated product stream separation of noble gases of 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
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • 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
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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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    • F25J3/04424—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 without thermally coupled high and low pressure columns, i.e. a so-called split columns
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04624—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon 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
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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
    • F25J3/04642—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
    • 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
    • F25J3/04642—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
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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
    • F25J3/04642—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
    • F25J3/04703—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 being arranged in more than one vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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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
    • 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.
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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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    • F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude oxygen")
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    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon

Definitions

  • the present invention relates to an air separation plant, a process for recovering an argon product by cryogenic separation of air, and a process for producing a corresponding air separation plant.
  • argon can be recovered in conventional air separation plants with known double column nitrogen-oxygen separation systems and an additional argon recovery unit.
  • argon accumulates in the region of the so-called argon transition in the low-pressure column (also referred to as the argon belly or argon bubble), where it reaches concentrations in the gas phase of up to 15%.
  • an argon-enriched stream is withdrawn slightly below this maximum argon from the low pressure column, so that it has a lower nitrogen content.
  • the argon-enriched stream is transferred to a so-called crude argon column.
  • the crude argon column is a separation column for argon-oxygen separation.
  • the crude argon column may be formed by a one-piece column, but there are also two- or multi-part columns, for example in the EP 0 628 777 B1 , described.
  • Corresponding air separation plants are hardly any prefabricated, because the respective component groups usually can not be transported over longer distances. This means that they have to be created at the respective destination. This is disadvantageous for a variety of reasons, among others because appropriate personnel at the destination are either unavailable or expensive. The effort to create appropriate air separation plants thus increases significantly.
  • the invention is therefore based on the object to create an air separation plant of the type mentioned economically particularly favorable and operate.
  • the present invention proposes an air separation plant, a process for recovering an argon product by cryogenic separation of air and a method for producing a corresponding air separation plant with the features of the independent claims.
  • Preferred embodiments are the subject of the dependent claims and the following description.
  • an air separation plant which is set up for the production of an argon-containing product by low-temperature decomposition of compressed and cooled feed air.
  • the air separation plant has a high-pressure column, a multi-part low-pressure column and a multipart crude argon column.
  • the multi-part low-pressure column and the multi-part crude argon column each have at least one foot section and a head section arranged spatially separated therefrom.
  • the multi-part low-pressure column and the multi-part crude argon column are each formed in two parts.
  • the air separation plant operates on the basis of the principles explained above, wherein an argon-enriched stream of the low-pressure column of the air separation plant can be removed.
  • the "argon-containing product” can be, for example, liquid argon (LAR), gaseous argon (GAR, possibly obtained by so-called internal compression) or so-called fake argon (impure argon, which is added in gaseous form to a residual gas in the cold state) ,
  • LAR liquid argon
  • GAR gaseous argon
  • fake argon impure argon, which is added in gaseous form to a residual gas in the cold state
  • a "two-part" pillar is designed in such a way that the two sections (head section and foot section) can be arranged spatially separated from one another.
  • Known air separation plants for example, column systems for nitrogen-oxygen separation have, in which the high-pressure column and the low-pressure column are arranged separately from each other and connected heat exchangers via a top condenser. Such column systems are "formed in two parts”.
  • the term "two-part design” thus delimits corresponding configurations from structural units in which components are permanently connected to one another and can not be arranged separately from one another.
  • foot section and "head section” respectively designates the sections of the two-part columns which, in terms of their function, in particular with regard to the fractions or streams occurring there, correspond to the lowermost or uppermost sections of conventional, one-part columns.
  • a foot section has, for example, a sump container
  • a head section has, for example, a top condenser.
  • the head section is thus the part of the columns which is connected to a corresponding condenser, and in which a return to the corresponding columns is abandoned.
  • air separation plants an oxygen-rich liquid fraction is recovered in the sump, which can be withdrawn as an oxygen product. This also takes place in a sump of a foot section of a two-part low-pressure column.
  • a "multipartite" low-pressure and / or crude argon column has more than two parts, intermediate sections between the foot and head sections are additionally provided.
  • the individual sections foot, head and possibly intermediate sections are connected to one another by means of lines and, if appropriate, pumps, in order in this way to provide an operation as is also carried out with a respective one-part column.
  • the air separation plant according to the invention is configured in a conventional manner, which means that at least one oxygen-rich stream can be obtained in the high-pressure column from at least part of feed air, which can be provided, for example, in the form of a plurality of feed air streams.
  • the oxygen-rich stream can be converted at least partially into the multi-part low-pressure column, specifically in its foot section.
  • at least one argon-rich stream can be obtained from the so-called argon transition from at least part of the oxygen-enriched stream. This can be converted into the multi-part crude argon column, and initially also in the foot section.
  • at least one portion of the argon-enriched stream can be used to recover at least one argon-rich stream.
  • a “stream” is a fluid that is continuously carried in a corresponding conduit.
  • a “fraction” represents a proportion of a starting mixture, for example of air, which can be separated from the starting mixture. Such a fraction can be routed at any time as a current in a corresponding conduit system or in a column.
  • a stream or fraction may be " enriched " with respect to one or more contained components, wherein an enriched fraction or stream has a higher content of one or more appropriately designated components than the starting mixture.
  • an enrichment is present when the content corresponds to at least two, five, ten or one hundred times the corresponding content in the starting mixture.
  • a "rich" current relative to one or more components predominantly has the corresponding component (s).
  • an argon-rich stream at least 80%, 90%, 95% or 99% argon on a molar, weight or volume basis.
  • the air separation plant according to the invention is characterized in that at least one liquid stream can be transferred from a lower region of the head section of the low-pressure column and from a lower region of the foot section of the crude argon column by means of a common pump into an upper region of the foot section of the low-pressure column.
  • the invention may include different arrangements of the columns or their sections.
  • the foot portion and / or the head portion of the crude argon column may be arranged geodetically at least partially adjacent to the head portion of the low-pressure column.
  • the high-pressure column, the head section of the low-pressure column, the foot section and the head section of the crude argon column may also be arranged geodetically at least partially next to each other.
  • the foot portion or the head portion of the crude argon column is arranged geodetically completely above the head portion of the low-pressure column.
  • the foot portion of the low-pressure column are arranged in vertical plan view next to its head portion and the foot portion of the crude argon column in vertical plan view next to its head portion.
  • the foot portion or the head portion of the crude argon column is arranged geodetically completely above the head portion of the low pressure column, the high pressure column and the foot portion of the low pressure column on the one hand and the head portion or the foot portion of the crude argon column and the head portion of the low pressure column in vertical plan view at least partially stacked.
  • the "deepest point" of a column or a column portion is respectively the lowest point at the bottom of a bottom-side disposed container, for example, a sump container, or the entire interior of the column or the column portion. Any connected lines are not part of the column.
  • the "highest point” of a column or column section is the roof of the column or column section. If a column or column section has a top condenser, its highest point is the highest point of the column or column section.
  • An arrangement of a component "in vertical plan view next to” here means an arrangement in which the corresponding components are arranged side by side in vertical projection. This does not exclude that the corresponding elements are arranged at different (geodetic) heights to each other.
  • the foot portion of the low pressure column may be arranged in vertical plan view adjacent to the head portion of the low pressure column, but the height arrangement may be so different that the geodetically highest point of the head portion of the low pressure column is still below the geodesic lowest point of the foot portion of the low pressure column.
  • the components are arranged "in vertical top view at least partially one above the other"
  • their peripheral lines overlap at least in part. For example, a Rohargon constituteer be moved sideways in order to build space-saving.
  • the arrangement according to the invention in the mentioned embodiments proves to be particularly advantageous because in this way corresponding air separation plants can be created with significantly lower height.
  • an air separation plant with a crude argon column with an effective height of about 60 m by a corresponding division and arrangement in a total height of about 40 m are created.
  • the crude argon column with the said height is divided into, for example, two parts.
  • the head section of the likewise two-part low pressure column can be placed geodesically below the top or bottom section of the crude argon column in a common coldbox.
  • This arrangement has a number of additional advantages, which will be explained below.
  • the foot section of the low-pressure column can form a structural unit with the high-pressure column and, as such, can also be placed in a corresponding cold box.
  • the high-pressure column and the foot section of the low-pressure column can be connected to one another in a heat-exchanging manner via a main condenser. This configuration corresponds to a conventional air separation plant with a Linde double column.
  • the corresponding coldbox for the head or foot section of the crude argon column and the head section of the low-pressure column only measures approx. 40 m.
  • the transport is easier.
  • the remaining section of the crude argon column also requires a height of about 40 m.
  • the air separation plant can therefore be created particularly cost-effective and, in particular due to the mentioned pump arrangement according to the invention, operated.
  • such an air separation plant can be completely prefabricated at the production site and transported in the appropriate cold boxes in the form of modular units to the destination.
  • a complex connection of a variety of components at the destination is therefore not required.
  • the plant components can be easily and completely in the factory on their own Functionality are checked, which may be unnecessary complicated diagnostics of individual components at the destination.
  • the low-pressure column is in this case preferably designed and operated such that the mentioned argon transition is located at the separation point between the top and bottom sections of the low-pressure column.
  • an argon-enriched stream is withdrawn slightly below the actual maximum argon from the low pressure column, so that it has a lower nitrogen content. This can be taken into account when choosing the separation point and when operating the low-pressure column.
  • the streams from the bottom of the leg section of the crude argon column and from the bottom of the top section of the low pressure column have equal or similar argon concentrations so that they can be fed by the common pump into the top of the foot section of the low pressure column.
  • An air separation plant according to the invention can be produced in different configurations, in particular using so-called piping skids, that is to say of casing modules which also allow prefabricated piping.
  • the air separation plant according to the invention advantageously comprises a pure argon column, in which argon can be obtained with a purity in the range mentioned above.
  • the pure argon column can be arranged in one of the mentioned cold boxes or separately, in particular in its own cold box.
  • a process according to the invention comprises recovering an argon product by cryogenic separation of compressed and cooled feed air.
  • FIGS. 1 and 2 shown air separation plants are merely exemplary and that in particular the dimensions of the components shown there, in particular the columns, are not to scale.
  • the crude argon column of a corresponding air separation plant usually the greatest height, which is not reproduced to scale in the drawing.
  • dumbbells are known from which only argon is withdrawn in order to achieve an energy advantage. Such columns are significantly lower, ie lower than the other columns.
  • FIG. 1 an air separation plant according to the invention for obtaining an argon product is shown schematically and designated 100 in total.
  • the air separation plant has a high-pressure column 1, a two-part low-pressure column with a foot section 2 and a head section 3, a likewise two-part crude argon column with a foot section 4 and a head section 5 and a pure argon column 6 on.
  • the foot section 2 and the head section 3 of the low-pressure column are structurally separated from each other.
  • the head section 3 of the low-pressure column is arranged in vertical plan view next to the high-pressure column 1, the foot section 2 of the low-pressure column above.
  • the foot section 2 and the head section 3 of the low-pressure column together correspond functionally to a conventional low-pressure column of a Linde double column.
  • the high-pressure column 1 and the two column sections 2 and 3 of the low-pressure column thus form a distillation column system for nitrogen-oxygen separation.
  • cooled and compressed feed air in the form of two streams a and b is fed into the high-pressure column 1.
  • the currents a and b may be a so-called turbine current (current a) on the one hand and a so-called inductor current (current b) on the other hand.
  • the air separation plant 100 according to the invention can thus be designed for internal compression.
  • the provision of the streams a and b is for example in the EP 2 026 024 A1 shown.
  • atmospheric air can be sucked in via a filter from an air compressor and compressed there to an absolute pressure of 5.0 to 7.0 bar, preferably about 5.5 bar.
  • the air can also be compressed to a higher pressure in the air compressor itself or in a further compressor (secondary compressor) arranged downstream thereof and subsequently expanded by means of an expansion machine, whereby, for example, part of the refrigeration requirement of the air separation plant 100 can be covered.
  • the air can be cooled after compression, for example in a direct contact cooler in direct heat exchange with cooling water.
  • the cooling water may for example be supplied from an evaporative cooler and / or from an external source.
  • the compressed and cooled air can then be cleaned in a cleaning device. This may for example comprise a pair of containers which are filled with a suitable adsorption material, preferably molecular sieve.
  • the purified air is then, i.d.R. in a main heat exchanger, cooled to about dew point.
  • the operating pressures - respectively at the top and the top of the head section - are 4.5 to 6.5 bar, preferably about 5.0 bar in the high-pressure column 1 and 1.2 to 1.7 bar, preferably about 1.3 bar in the low pressure column 2, 3.
  • the foot section 2 and the head section 3 of the low pressure column are preferably operated at substantially the same pressure, but this does not exclude certain pressure differences, for example due to line resistance.
  • the high-pressure column 1 and the foot portion 2 of the low-pressure column are connected via a main capacitor 12 in heat exchanging connection and are designed as a structural unit.
  • the invention can also be used in systems in which the high-pressure column 1 and the low-pressure column (or their foot section 2) are arranged separately from one another and have a separate, ie. not integrated into the columns, have main capacitor.
  • Air that is liquefied in feeding the feed air stream b into the high pressure column 1 may be partially removed as a corresponding stream c, heated in a subcooler countercurrent 13, and then otherwise used or recompressed and provided as feed air stream a, b.
  • An oxygen-enriched fraction d is withdrawn from the bottom of the high-pressure column 1, subcooled in the subcooling countercurrent 13 and further cooled as stream e to a part in a bottom evaporator 14 of the pure argon column 6. Another part can be routed past the bottom evaporator 14. A portion of the stream e flows into the evaporation space of a top condenser 15 of the head section 5 of the two-part crude argon column, another part in the evaporation space of a top condenser 16 of the pure argon column 6. The proportion of the oxygen-enriched fraction evaporated in the top condensers 15 and 16 is as stream f the head portion 3 of the low pressure column supplied at a first intermediate point. The remaining liquid portions are given as stream g at a second intermediate point of the head section 3 of the low-pressure column, which is above the first intermediate point.
  • Gaseous nitrogen from the top of the high-pressure column 1 can be heated as a stream h, for example in the main heat exchanger, not shown, for cooling the feed air to about ambient temperature and then, for example, as in the EP 2 026 024 A1 presented, further treated.
  • the remaining gaseous nitrogen from the top of the high-pressure column 1 is at least partially condensed in the main condenser 12.
  • the liquid nitrogen produced in this process is partly applied to the high-pressure column 1 as reflux.
  • Another part, after subcooling in the subcooling countercurrent 13, is passed as a stream i to the upper part of the head section 3 of the low pressure column.
  • a gaseous stream of nitrogen j from the head of the head section 3 of the low-pressure column can be used in different ways after passing through the subcooling countercurrent 13 or used further in the air separation plant.
  • a liquid oxygen stream k from the sump of the foot section 2 of the low-pressure column can be brought to liquid pressure by means of a pump 17 and subsequently supplied to, for example, a liquid oxygen tank (LOX). Part of this oxygen can also be vaporized to provide gaseous pressure oxygen (so-called internal compression).
  • LOX liquid oxygen tank
  • the division of the low-pressure column into the foot section 2 and the head section 3 and their operation are carried out in such a way that an argon-enriched fraction accumulates in the lower part of the head section 3 of the low-pressure column.
  • This is the area of the so-called argon transition (also referred to as argon belly or argon section).
  • This enrichment results from the volatility of argon, which is between that of nitrogen and that of oxygen.
  • the argon transition is above and below the intermediate point at which an oxygen-enriched fraction is fed (streams f and g).
  • Argon concentrations of up to 15% in the vapor phase can be achieved.
  • the argon-enriched stream is usually withdrawn below this intermediate point, as is the case here (stream m).
  • a current I flows from the upper part of the foot section 2 of the low-pressure column into the head section 3 of the low-pressure column in its lower region, whereby the foot section 2 and the head section 3 of the low-pressure column are partially functionally coupled.
  • an argon-rich stream m is withdrawn from the head section 3 of the low-pressure column and fed into the foot section 4 of the crude argon column.
  • the feed takes place immediately above the bottom of the foot section 4 of the crude argon column.
  • Bottom liquid from the bottom of the head section 3 of the low-pressure column and from the bottom of the leg section 4 of the crude argon column is returned via a pump 18 as stream n into the root section 2 of the low-pressure column.
  • the top condenser 15 of the head portion 5 of the crude argon column may be formed as a reflux condenser. Gas from the top of the head portion 5 of the crude argon column flows down into the return passages where it is partially condensed. The condensate generated in this case flows in countercurrent to the rising gas in the return passages down and is used in the head section 5 of the crude argon column as a liquid reflux. On the evaporation side, the top condenser 15 is designed as a bath condenser.
  • the cooling fluid which is formed here by the liquid oxygen-enriched fraction from the high-pressure column 1, flows down through one or more lateral openings in the evaporation passages and is partially evaporated there.
  • Liquid is entrained by the thermosiphon effect, exits along with the vaporized portion at the top of the evaporation passages, and is returned to the liquid bath.
  • the top condenser 15 is thus formed on the evaporation side as a bath evaporator.
  • a crude argon stream n is taken off in gaseous form via a lateral header and fed to the pure argon column 6 at an intermediate point.
  • the top condenser 16 of the pure argon column 6 is conventionally designed in the example on the liquefaction side, ie a top gas stream o of the pure argon column 6 flows from top to bottom through the liquefaction passages.
  • the top condenser 16 of the pure argon column 6 and / or the main condenser 12 could be designed as reflux condenser.
  • a residual gas stream p is withdrawn and blown off into the atmosphere (ATM) in the example.
  • ATM atmosphere
  • it can be returned via its own fan in the high-pressure column 1 or the low-pressure column 2, 3 and / or in front of the air compressor.
  • the bottom liquid of the pure argon column 6 is partially evaporated as stream p in the bottom evaporator 14 and the steam generated is used as ascending gas in the pure argon column 6. The remainder is taken as liquid pure argon product stream q (LAR).
  • FIG. 1 An exemplary integration of the components of the air separation plant 100 in corresponding cold boxes is in the FIG. 1 illustrated by dashed lines.
  • A designates a first cold box, which is set up to receive the high-pressure column 1 and the foot section 2 of the low-pressure column.
  • a second cold box B can be set up for receiving the head section 3 of the low-pressure column.
  • a third cold box C is adapted to receive the head section 5 of the crude argon column.
  • the head section 3 of the low-pressure column and the head section 5 of the high-pressure column can also be arranged in a common coldbox.
  • Such a cold box may for example have a height of 40 m.
  • a fourth coldbox D is shown reduced in size in the illustrated example and, for example, also has a height of 40 m.
  • FIG. 2 an air separation plant for obtaining an argon product according to a further embodiment of the invention is shown even more schematically.
  • this air separation plant only the columns 2 to 6 are shown, on a representation of the corresponding compounds, pumps and heat exchangers was largely dispensed with.
  • a foot section 4 of the crude argon column is arranged above the head section 3 of the low-pressure column.
  • the subdivision of the crude argon column can be made at a different location than shown in the figure, if this is expedient for the arrangement according to the invention.
  • fluid from the foot section 4 of the crude argon column and the head section 3 of the low-pressure column can be pumped by the pump 18 as stream n in the foot section 3 of the low-pressure column.
  • the foot section 4 and / or the head section 5 of the crude argon column is arranged geodetically at least partially adjacent to the head section 3 of the low-pressure column.
  • all column sections 1 to 4 can be arranged at least partially geodetically next to each other.
  • the diameter of the columns can be influenced accordingly by the choice of internals in the respective columns (sieve trays, packings with different densities) and, if necessary, a further structural adaptation can be achieved.

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  • Mechanical Engineering (AREA)
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EP14716232.5A 2013-03-06 2014-03-05 Luftzerlegungsanlage, verfahren zur gewinnung eines argon enthaltenden produkts und verfahren zur erstellung einer luftzerlegungsanlage Active EP2965029B1 (de)

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EP14716232.5A EP2965029B1 (de) 2013-03-06 2014-03-05 Luftzerlegungsanlage, verfahren zur gewinnung eines argon enthaltenden produkts und verfahren zur erstellung einer luftzerlegungsanlage

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EP3614082A1 (de) 2018-08-22 2020-02-26 Linde Aktiengesellschaft Luftzerlegungsanlage, verfahren zur tieftemperaturzerlegung von luft und verfahren zur erstellung einer luftzerlegungsanlage
WO2020038608A1 (de) * 2018-08-22 2020-02-27 Linde Aktiengesellschaft Luftzerlegungsanlage, verfahren zur tieftemperaturzerlegung von luft und verfahren zur erstellung einer luftzerlegungsanlage
WO2022258222A1 (de) 2021-06-07 2022-12-15 Linde Gmbh Luftzerlegungsanlage und luftzerlegungsverfahren
WO2023001400A1 (de) 2021-07-22 2023-01-26 Linde Gmbh Pumpenmodul für eine luftzerlegungsanlage, luftzerlegungsanlage und verfahren zum aufbau
WO2023030683A1 (de) 2021-09-01 2023-03-09 Linde Gmbh Anlage und verfahren zur tieftemperaturzerlegung von luft
WO2023030682A2 (de) 2021-09-01 2023-03-09 Linde Gmbh Anlage und verfahren zur tieftemperaturzerlegung von luft

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JP2016515188A (ja) 2016-05-26
CN105026862A (zh) 2015-11-04
CA2900122C (en) 2023-10-31
US20150369535A1 (en) 2015-12-24
WO2014135271A2 (de) 2014-09-12
EP2965029A2 (de) 2016-01-13
US10591209B2 (en) 2020-03-17
WO2014135271A3 (de) 2015-01-08
CA2900122A1 (en) 2014-09-12
BR112015020093A2 (pt) 2017-07-18
RU2015142384A (ru) 2017-04-10
JP6257656B2 (ja) 2018-01-10
KR20150126001A (ko) 2015-11-10
CL2015002367A1 (es) 2016-03-04
CN105026862B (zh) 2018-03-27
RU2659698C2 (ru) 2018-07-03
KR102178230B1 (ko) 2020-11-12

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