WO2020187449A1 - Procédé et installation de décomposition d'air à basse température - Google Patents

Procédé et installation de décomposition d'air à basse température Download PDF

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Publication number
WO2020187449A1
WO2020187449A1 PCT/EP2020/025125 EP2020025125W WO2020187449A1 WO 2020187449 A1 WO2020187449 A1 WO 2020187449A1 EP 2020025125 W EP2020025125 W EP 2020025125W WO 2020187449 A1 WO2020187449 A1 WO 2020187449A1
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Prior art keywords
column
liquid
fed
gas
pressure range
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PCT/EP2020/025125
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German (de)
English (en)
Inventor
Tobias Lautenschlager
Dimitri GOLUBEV
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Linde Gmbh
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Publication of WO2020187449A1 publication Critical patent/WO2020187449A1/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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
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    • 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
    • F25J3/0406—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 of nitrogen
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    • F25J3/04096—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 argon or argon enriched stream
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
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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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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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
    • 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
    • F25J2200/10—Processes or apparatus using separation by rectification in a quadruple, or more, column or pressure 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
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of 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
    • 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
    • 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
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams

Definitions

  • the present invention relates to a method and a system for
  • Air separation plants have rectification column systems that
  • Multi-column systems can be formed.
  • rectification columns for obtaining nitrogen and / or oxygen in liquid and / or gaseous state, i.e. the rectification columns for nitrogen-oxygen separation
  • rectification columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • the terms “rectification” and “distillation” and “column” and “column” or terms composed of these are often used synonymously.
  • EP 1 227 288 A1 uses a three-column system which has a high pressure column, a low pressure column and an intermediate column. Feed air is introduced into the high pressure column and there into a first one
  • At least part of the first nitrogen fraction is in a first
  • Condenser evaporator condensed to a first liquid nitrogen fraction.
  • a first oxygen-enriched fraction from the high pressure column is fed into the
  • the intermediate column is introduced into the low-pressure column, where it is separated into a third oxygen-enriched liquid and a third nitrogen fraction. Liquid reflux nitrogen that has not been formed in the second condenser-evaporator is introduced into the intermediate column.
  • the rectification columns of the mentioned rectification column systems are operated at different pressure levels.
  • Known double column systems have a so-called high pressure column (also referred to as a pressure column, medium pressure column or lower column) and a so-called low pressure column (also referred to as an upper column).
  • the high pressure column is typically operated at a pressure level of 4 to 7 bar, in particular approx. 5.3 bar.
  • the low-pressure column is operated at a pressure level of typically 1 to 2 bar, in particular about 1.4 bar. In certain cases, both
  • Rectification columns can also be used at higher pressure levels.
  • the pressures given here and below are absolute pressures at the top of the respective columns given.
  • liquid argon can be delivered or evaporated on site, or gaseous argon can be obtained on site.
  • the delivery of liquid argon not only brings economic disadvantages (transport costs, refueling losses, cold losses when evaporating against ambient air), but also makes high demands on the
  • Air separation plants are typically used to extract argon
  • Rectification columns are designed accordingly. Pure argon can then be withdrawn from the crude argon column or a comparable column, typically somewhat further below than the fluid conventionally transferred into the pure argon column.
  • the present invention therefore sets itself the task of specifying a method and an air separation plant by means of which, in addition to larger amounts of high-purity, gaseous nitrogen on a clearly Above-atmospheric pressure level, argon can also be provided in an advantageous manner.
  • Liquids and gases can be rich or poor in one or more components in the parlance used here, with “rich” for a content of at least 75%, 90%, 95%, 99%, 99.5%, 99.9% or 99.99% and “poor” can mean a content of no more than 25%, 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis.
  • the term “predominantly” can match the definition of "rich”.
  • Liquids and gases can also be enriched or depleted in one or more components, these terms referring to a content in a starting liquid or a starting gas from which the liquid or the gas was obtained. Be the liquid or the gas
  • pressure range and “temperature range”, which is intended to express that corresponding pressures and temperatures in a corresponding system do not have to be used in the form of exact pressure or temperature values in order to implement the inventive concept. However, such pressures and temperatures typically move in certain ranges, for example ⁇ 1%, 5% or 10% around a mean value.
  • pressure ranges and temperature ranges can be in disjoint areas or in areas that overlap one another.
  • pressure ranges include, for example, unavoidable or expected pressure losses.
  • temperature ranges The values specified in bar for the pressure ranges are absolute pressures.
  • expansion machines are mentioned here, this is typically understood to mean known turboexpander. These expansion machines can in particular also be coupled to compressors. These compressors can in particular be turbo compressors. A corresponding combination of turbo expander and turbo compressor is typically also referred to as a "turbine booster".
  • turbine booster the turbo-expander and the turbo-compressor are mechanically coupled, the coupling being able to take place at the same speed (for example via a common shaft) or at different speeds (for example via a suitable transmission gear).
  • compressor is used here in general.
  • a “cold compressor” here denotes a compressor to which a fluid flow is fed in a temperature range well below 0 ° C, in particular below -50, -75 or -100 ° C and down to -150 or -200 ° C. A corresponding fluid flow is cooled to a temperature in this temperature range in particular by means of a main heat exchanger (see below).
  • a “main air compressor” is characterized by the fact that it compresses all of the air that is fed to the air separation plant and separated there. In contrast, in one or more optionally provided further compressors, for example booster compressors, only a portion of these is already previously in the main air compressor compressed air further compressed.
  • the "main heat exchanger" of an air separation plant represents the heat exchanger in which at least the
  • a “heat exchanger” for use in the context of the present invention can be designed in a manner customary in the art. It serves for the indirect transfer of heat between at least two e.g. fluid flows guided in countercurrent to one another, for example a warm compressed air flow and one or more cold ones
  • Fluid flows or a cryogenic liquid air product and one or more warm or warmer, but possibly also cryogenic fluid flows.
  • Heat exchanger can be formed from a single or several heat exchanger sections connected in parallel and / or in series, e.g. from one or more plate heat exchanger blocks. For example, it is one
  • Such a heat exchanger has "passages" which are separated from each other as fluid channels
  • Heat exchange surfaces are formed and connected in parallel and separated by other passages to form "passage groups". Characteristic of a
  • the heat exchanger is that in it heat is exchanged between two mobile media at a time, namely at least one fluid flow to be cooled and at least one fluid flow to be heated.
  • a “condenser evaporator” is a heat exchanger in which a first, condensing fluid flow enters into indirect heat exchange with a second, evaporating fluid flow.
  • Each condenser evaporator has one
  • Evaporation chambers have liquefaction or evaporation passages.
  • the condensation (liquefaction) of the first fluid flow is carried out in the liquefaction space, and the evaporation of the second fluid flow in the vaporization space.
  • the evaporation and the liquefaction space are formed by groups of passages which are in a heat exchange relationship with one another.
  • a "forced flow" condenser evaporator is a liquid or
  • the gas-liquid mixture emerging from the evaporation chamber is passed on in a "once through" condenser evaporator of this type, separated according to phases, directly to the next process step or to a downstream device and in particular not into a
  • Components "one above the other” is understood here to mean that the upper end of the lower of the two components is at a lower or the same geodetic height as the lower end of the upper of the two components and that the projections of the two apparatus parts intersect in a horizontal plane.
  • the two components are arranged exactly one above the other, that is, the axes of the two components run vertically on the same
  • the axes of the two components do not have to be exactly perpendicular, but can also be offset from one another, especially if one of the two components, for example a rectification column or a column part with a smaller diameter, is to have the same distance from the sheet metal jacket of a coldbox as another with a larger one Diameter.
  • the present invention proposes a method for
  • Double column system emerges, as explained in detail below.
  • the third column can be provided in particular structurally separate from the first and second column, wherein the first and second column can in particular be part of a double column and by means of a corresponding one Condenser evaporator, the so-called main condenser, which is referred to here as the "first" condenser evaporator, can be in heat-exchanging connection with one another.
  • the main condenser which is referred to here as the "first" condenser evaporator
  • different ones can also be used
  • first and the second column which are part of a
  • Double columns are formed, can also be supplemented by an additional column in a corresponding multiple column system, or the second and third columns can be provided as separate columns.
  • the main capacitor can be provided as an internal or external main capacitor, as is basically known from the prior art. If an internal main condenser is used, this is at least partially submerged in a bottom liquid in the bottom of the second column, as is the case in an embodiment of the invention described below, and an overhead gas to be condensed from the second column is passed through a condensation chamber of the
  • the fourth column in the context of the present invention serves in particular to extract argon or discharge argon from a gas mixture which is withdrawn from the third column.
  • the fourth column can in particular be a crude argon column of a known arrangement with crude and pure argon column, but it can also be a modified argon column that can contain several argon in the pure state without the use of an additional pure argon column theoretical trays below the head is taken. Other variants are also possible within the scope of the present invention.
  • the first column is operated in a first pressure range
  • the second column is operated in a second pressure range below the first pressure range
  • the third column is operated in a third pressure range below the second (and thus also the first) pressure range.
  • the fourth column is also operated in the third pressure range, the operating pressure in the fourth column in particular being able to be slightly below the operating pressure of the third column, which is particularly evident
  • the first pressure range can in particular be 9 to 12 bar, for example approx. 10.5 bar.
  • the second pressure range is advantageously 4 to 6 bar, in particular approximately 5.5 bar, and the third
  • the pressure range is advantageously 1 to 2 bar, in particular approx. 1.4 bar.
  • the pressure specifications here denote absolute pressures at the head of corresponding columns.
  • the second and third columns are thus operated in the context of the present invention, as already mentioned above, in pressure ranges in which the high and low pressure columns conventionally used in air separation plants are also operated.
  • the first column is operated in a higher pressure range.
  • the first and second columns, which are advantageously combined to form a double column, are therefore, in one embodiment of the invention, structurally comparable, if necessary, as in a double column
  • Conventional air separation plant arranged, but are operated at corresponding higher pressure levels.
  • the first column is operated at a higher (first) pressure level than a conventional high pressure column and the second column is operated at a higher (second) pressure level than a conventional low pressure column.
  • the bottom liquid of the second column with a higher oxygen content and a higher argon content than the
  • the bottom liquid of the first column is formed and the bottom liquid of the third column has a higher oxygen content and a lower argon content formed as the bottom liquid of the second column.
  • the higher argon content of the bottom liquid of the second column compared to that of the bottom liquid of the first column results from the different operating conditions, in particular the different pressures that are used to operate the first and second columns, as well as from different compositions of material flows that enter the first and second column are fed.
  • the lower argon content results in the bottom liquid of the third column
  • the oxygen content of the bottom liquid of the first column is hereinafter also referred to as the "first" oxygen content
  • the oxygen content of the bottom liquid of the second column is also referred to as the "second" oxygen content
  • the first oxygen content can be at 28 to 40%, in particular at approx. 34%, the second oxygen content at approx. 45 to 90%, in particular at approx. 80%, and the third oxygen content at approx. 0 to 99.99%, in particular around 99.5%.
  • the respective percentages relate to the molar content of oxygen in a corresponding one
  • the third column is therefore used in the context of the present invention as a pure oxygen column and a corresponding pure oxygen product can be withdrawn from it.
  • the first and the second sump liquid are typically not used as a product, but are further processed in the plant.
  • fluid from the first column is generally fed into the second column and optionally also into the third column, fluid from the second column is fed into the third column, fluid from the third column is fed into the fourth column, and Fluid from the fourth column is fed into the third column.
  • fluid is fed from one column into another, this is to be understood in particular as a direct or indirect transfer of a corresponding fluid flow.
  • the transfer of the corresponding fluids can initially also be carried out in one feed
  • the transferred fluids can include overhead gases, bottom liquids and / or side streams of corresponding columns. Under a "side stream" is a
  • a bottom liquid is discharged from the respective column in particular in the form of a liquid substance flow, and a top gas in particular in the form of a gaseous substance flow.
  • a top gas in particular in the form of a gaseous substance flow.
  • a side stream can be in a liquid or gaseous state.
  • a liquid side stream can, for example, from a
  • Liquid retention device or taken from a storage floor.
  • the fluid fed from the third column into the fourth column comprises at least part of a side stream which has a lower oxygen content and a higher argon content than that
  • Bottom liquid is withdrawn from the third column.
  • the side stream is withdrawn from the third column in particular in the area of the argon transition already explained above, but it can also be withdrawn below the argon transition.
  • a corresponding side stream is in particular a gas mixture which has a higher argon content than the bottom liquid and a lower argon content than the top gas of the third column and is therefore similar to a side stream that is obtained in a conventional process from FIG
  • Low pressure column is transferred into the crude argon column.
  • the top gas of the first column ie the entire top gas or only a part thereof
  • the top gas of the first column is subjected to a condensation against bottom liquid of the second column and is returned in liquid form to the first column.
  • This can also include that a partial condensation of the top gas is carried out and only the liquid phase formed or a part thereof is returned to the first column.
  • bottom liquid from the third column is discharged from the air separation plant as an oxygen-rich product with the oxygen contents already explained in more detail above.
  • the invention is characterized in that the top gas of the second column (here too, the entire top gas or part thereof) is subjected to a condensation against further bottom liquid of the second column and is returned in liquid form to the second column.
  • the respective proportions of the bottom liquid of the second column used in the condensation are used in particular in the manner explained below in corresponding condenser evaporators.
  • the present invention allows a total recovery of over 70% of the argon contained in the process air as a product among those mentioned at the beginning
  • a method as proposed according to the invention can be used to efficiently provide pressurized nitrogen with simultaneous argon production without the disadvantages mentioned at the beginning.
  • the pressurized nitrogen can in particular comprise non-condensed further top gas of the first column which is already at a suitable pressure (in the first pressure range) and can be discharged from the air separation plant at this pressure.
  • the corresponding pressurized nitrogen can additionally also include non-condensed further top gas of the second column, which is only present at a pressure in the second pressure range, but in particular compressed on the warm side of the main heat exchanger of the air separation plant to a pressure in the first pressure range and then to the heated top gas from the first column can be fed.
  • a common compressor can in particular be used, which also compresses a circulating flow formed in the air separation plant, as explained below.
  • top gas from the third column For the purpose of providing a nitrogen product, it is also possible, in particular, to use top gas from the third column. Furthermore, within the scope of the present invention, further top gas from the second column or other gas from the first column or the second column (for further details see below) is subjected to condensation against further bottom liquid from the third column and returned to the second column.
  • Bottom liquid of the third column is condensed, a side stream withdrawn from the first column or from the second column can be used.
  • a corresponding side stream which is withdrawn from the first column and condensed against the further bottom liquid of the third column, can be one beforehand
  • Turbine relaxation is subjected from a pressure in the first pressure range to a pressure in the second pressure range.
  • the use of such a turbine expansion can in particular produce cold.
  • Turbine expansion of this type can in particular be carried out in a so-called pressurized nitrogen turbine or PGAN turbine. If instead a side stream is withdrawn from the second column and condensed against the further bottom liquid of the third column, this side stream can also be subjected beforehand to a corresponding turbine expansion. In both cases, the
  • the present invention is distinguished in particular by the specific arrangement of condenser evaporators in or opposite the first of the second and third columns.
  • a first condenser-evaporator is used for the condensation of the top gas of the first column against the bottom liquid of the second column, which is arranged above the first column and / or in a bottom region of the second column. This can in particular be the one mentioned
  • a second condenser-evaporator is advantageously used for the condensation of the top gas of the second column against the further bottom liquid of the second column used, which is arranged above the second column, and for the condensation of the further top gas from the second column or the other gas from the first column or the second column against the further bottom liquid of the third column, a third condenser evaporator is advantageously used, which is in a The bottom area of the third column is arranged.
  • the further bottom liquid of the second column is partially or completely evaporated.
  • the evaporated sump liquid is heated in particular after its evaporation, in particular in the main heat exchanger of the air separation plant, and discharged from the air separation plant.
  • the evaporated sump liquid can, since it has already been purified, in particular as a regeneration gas in a known
  • Adsorber unit are used. Since the evaporated sump liquid at a pressure in a comparatively high pressure range, for example a
  • This turbine expansion in a so-called residual gas turbine can take place in particular and after partial heating in the main heat exchanger.
  • the correspondingly expanded gas can then be further heated in the main heat exchanger.
  • a column system with a fifth column can be used, which is operated in an intermediate pressure range between the first pressure range and the third pressure range, the first column and the fifth column being fed with compressed air and a fifth column in the fifth column Sump liquid is formed.
  • the intermediate pressure range is in particular 4 to 6 bar.
  • the third column can in particular be provided as the upper part of a double column, in which case the fifth column can be provided as the lower part of the double column.
  • the compressed air used to feed the fifth column can initially be compressed to a pressure in the first pressure range, a first portion of this compressed air at this pressure in the first column fed and a second proportion of this compressed air to a pressure in the
  • bottom liquid from the fifth column can be fed into the third column, at least part of the bottom liquid from the fifth column, which is fed into the third column, at least against overhead gas from the fourth before being fed into the third column Column is subjected to partial evaporation.
  • Top gas of the fourth column and, as explained immediately, also top gas of a pure argon column, if present, can in this embodiment be condensed against the bottom liquid of the fifth column and returned to the fourth column and possibly the pure argon column.
  • bottom liquid from the first column or other liquid from the first column can be used against at least the top gas of the fourth column (and, if present, also against the top gas of a Pure argon column) can be subjected to partial evaporation, in which case a gas formed during partial evaporation is fed into the second column.
  • the gas formed during the partial evaporation can be heated before being fed into the second column, compressed to a pressure in the second pressure range and cooled again.
  • a main heat exchanger in particular can be used for heating and cooling
  • the nitrogen-rich product stream can in particular be the previously mentioned, uncondensed and heated further top gas from the second column, which is heated in the main heat exchanger and which can then be fed to likewise heated, uncondensed, further top gas from the first column.
  • a compressor is used for feed gas in the second column (hereinafter the
  • feed gas compressor also referred to as a "feed gas compressor"
  • the feed gas is formed from liquid evaporated as explained above, which is withdrawn from the first column.
  • a feed gas cycle is thus created, which is a cycle because the gas originates from the column system and is fed back into the column system.
  • the second column can in particular also be fed with compressed air, i.e. the feed gas originating from the feed gas circuit does not necessarily represent the entire feed gas in the second column.
  • a common feed air quantity can initially be brought to a pressure in the first pressure range.
  • a first partial stream of this common amount of feed air can be fed to the main heat exchanger on the warm side and removed on the cold side and, while still at a pressure in the first pressure range, fed into the first column.
  • a second part of this common feed air quantity can be fed to the main heat exchanger on the warm side, in particular after a previous further pressure increase, but can be withdrawn at an intermediate pressure level.
  • the second partial flow can then be subjected to the turbine expansion mentioned, specifically to a pressure in the second pressure range. It can then be fed into the second column at this pressure.
  • Turbine relaxation can be done, for example, using a braked turbine, for example a generator turbine or a turbine with an oil brake, but also in a booster turbine, with the mentioned further pressure increase of the second partial flow being able to be carried out in a booster of the booster turbine.
  • the gas carried in the feed gas circuit is in the feed gas compressor from a pressure of, for example, approx. 1.1 to 1.2 bar (the first bottom liquid is expanded into the respective condensation chambers) to a pressure of, for example, approx. 5 to 5.5 bar (or a pressure in the second pressure range) compressed.
  • the joint compression of a nitrogen product stream from the second column appears particularly favorable. The latter takes place in particular in one stage and from a pressure in the second pressure area to a pressure in the first
  • Nitrogen product of about 1.70 and an argon yield of 73.8%.
  • Low pressure nitrogen is a bonus product. Further adjustments (e.g. higher argon production with higher energy consumption and vice versa) are possible.
  • subcooling can be used at different positions within the scope of the present invention.
  • Process can in particular one or more fluids that are fed into the first column, into the second column and / or into the third column, against one or more fluids that are fed from the first column, from the second column and / or from the third Removed from the column, be subcooled.
  • Separate heat exchangers or a common heat exchanger can be used here, in particular the already mentioned subcooling counterflow.
  • top gas of the fourth column is condensed by means of a first condenser evaporator, in which a portion of the first
  • Partial evaporation is subjected.
  • This other liquid can be withdrawn from the first column in particular above the bottom.
  • a top condenser of a crude argon column or the only existing argon column is cooled using bottom liquid from the first column or another liquid.
  • This top gas can in particular then be fed into the third column.
  • a pure argon column is available as the fifth column, its top condenser can also be cooled using a corresponding bottom liquid, as explained below. According to an advantageous development of the method just explained, vaporized portions of the bottom liquid from the first column, in the top condenser or condensers of the fourth column or the fourth column and the
  • Pure argon column were used, then transferred to the second column, at a position that corresponds to the oxygen content and argon content of these fluids.
  • the vaporized fractions can therefore be fed into the second column at essentially the same point.
  • the streams mentioned can be combined or transferred separately from one another into the second column, and in particular after they have been previously heated and compressed.
  • the fluid transferred from the first column into the second column thus includes corresponding
  • Liquid i.e. at least part of the first sump liquid or others
  • the third column in particular can be fed with the non-evaporated liquid.
  • Adsorption unit for removing water and / or carbon dioxide from the
  • Process fed, compressed feed air are operated with a regeneration gas, which is at least a part of the top gas of the third column. In this way, the outlet pressure of the turbine, which is in a
  • the evaporation chamber of the second condenser evaporator is relaxed, lowered and additional cold is generated.
  • Expansion turbines are used, these are consumed by a cold compressor for a nitrogen product with a corresponding saving in compression power. Compression in a cold compressor is energetically advantageous.
  • liquid from the second column which is withdrawn from the second column in the form of a side stream, is transferred into the third column.
  • the feeding into the third column takes place in particular directly, i.e. especially without the composition
  • the withdrawal from the second column takes place advantageously at a position between the 3rd and the 14th theoretical plate, particularly advantageously between the 5th and 12th theoretical plate above the bottom of the second column.
  • the liquid is therefore highly enriched in oxygen, but the oxygen content is lower than the bottom liquid of the second column.
  • Air separation plant set up to carry out a method, as previously explained in different configurations, and this has means set up in each case for this purpose.
  • Air separation plant is expressly referred to the explanations relating to the method according to the invention.
  • Air separation plants according to FIGS. 1 to 11 are each designated as a whole by the reference numerals 1001 to 1011. Although the following
  • All of the air separation plants 1001 to 1011 shown in FIGS. 1 to 11 are equipped with a column system which, regardless of the different configuration and possibly different number of columns, is each designated as a whole by 10.
  • separating devices such as separating sections, separating trays and the like illustrated.
  • the columns each have corresponding separation devices and that these are each available in a suitable design and number to fulfill the respective separation tasks.
  • separating sections can be arranged in such a way that fluids can be fed in and removed in each case between corresponding separating sections (or above or below them in the case of the top and bottom of the columns).
  • a separating section is in each case an essentially continuous area of ordered or unordered packs.
  • the column systems 10 each have a first column 11 (for example with a plurality of horizontal dividing trays) and a second column 12
  • the first column 11 and the second column 12 are each designed as parts of a double column of a basically known type.
  • express reference is made to the technical literature on air separation plants cited at the beginning, in particular to the explanations on Figure 2.3A in Häring (see above), in which a corresponding double column is shown.
  • the first column 11 and the second column 12 are via one
  • Condenser-evaporator 111 the so-called main condenser, connected to one another in a heat-exchanging manner, which is used for the condensation of top gas of the first column 11 and is arranged in a sump area of the second column 12.
  • This condenser evaporator 111 is also referred to here as the “first” condenser evaporator.
  • the third column 13 is formed separately from the first column 11 and the second column 12.
  • the first column 11 is in a previously explained first pressure range
  • the second column 12 in a previously explained second pressure range below the first pressure range
  • the third column 13 in a third pressure range below the second pressure range operated.
  • the fourth column 14 is in particular also operated in the third pressure range. Bottom liquids and top gases are formed in the first column 11, the second column 12 and the third column 13.
  • the fourth column 14 is used in all air separation plants 1001 to 1011 according to FIGS. 1 to 11 for the extraction of argon.
  • the fourth column 14 is designed as a crude argon column and there is a separate pure argon column 16 in each of the air separation plants 1001 to 1008 according to FIGS. 1 to 8. If a Reinarkon column 16 is present, the fourth column is therefore called
  • Pure argon column 16 is dispensed with and pure argon can instead be withdrawn from the fourth column 14 if the above-explained requirements are met.
  • the air separation plants 1001 to 1008 shown there are each sucked in a feed air flow a by means of a main air compressor 1 via a filter, shown in hatched lines, which is not specifically designated a direct contact cooler 2, which is operated with cooling water W, and purified in an adsorption unit 3.
  • a filter shown in hatched lines, which is not specifically designated a direct contact cooler 2, which is operated with cooling water W, and purified in an adsorption unit 3.
  • FIGS. 9 to 11 only the correspondingly provided, compressed and purified feed air flow a is shown.
  • partial flows b and c are formed using air from the feed air flow a.
  • a further partial flow d is also formed.
  • the partial flows b and c are each supplied on the warm side to a main heat exchanger 4, the partial flow c previously being further compressed in a booster of a booster turbine arrangement 5.
  • the substream b is withdrawn from the main heat exchanger 4 on the cold side and into the first column 11 fed.
  • the substream c is the main heat exchanger 4 on a
  • Booster turbine arrangement 5 expanded and fed into second column 12.
  • the partial flow b is treated as explained for the air separation plants 1001 to 1008 shown in FIGS. 1 to 8, but there is a further partial flow b 'which is also treated accordingly and in particular the throttle is expanded in the first column 11.
  • the partial flow c is not compressed here before it
  • Main heat exchanger 4 is supplied on the warm side. However, if necessary, a corresponding compression can also be provided.
  • the partial flow c is taken from the main heat exchanger 4 at an intermediate temperature level and expanded in a turbine, which in the example shown is part of a
  • Generator turbine assembly 5 ' is.
  • the correspondingly expanded partial flow c is heated in the air separation plant 1009 according to FIG. 9 and in the air separation plant 1011 according to FIG. 11 in the main heat exchanger 4 and then transferred to the
  • the expanded substream is fed into a fifth column 15 (for example with one to three separating sections) which is operated in a pressure range which is referred to here as the "intermediate pressure range".
  • fluid is transferred from the first column 11 into the second column 12 or into the second column 12 and third column 13, from the second column 12 into the third column 13, fed from the third column 13 into the fourth column 12 and from the fourth column 14 into the third column 13.
  • the fluid fed into the fourth column 14 from the third column 13 in each case comprises at least a part of a side stream that has a lower oxygen content and a higher one
  • Argon content is withdrawn from the third column 13 as the third bottom liquid. Furthermore, in all configurations of the air separation plants 1001 to 1011 according to FIGS. 1 to 11, overhead gas from the first column 11 is subjected to condensation in a ("first") condenser evaporator 111 and then returned in liquid form to the first column 11 and overhead gas from the second column 12 becomes one
  • a (“third”) condenser evaporator 131 is used in the embodiments of
  • a side stream of the first or second column, which in particular can be turbine expanded beforehand, is condensed in this third condenser evaporator.
  • Air separation plant 1002 to 1011 only the features that differ in each case are explained.
  • the first bottom liquid is formed, from which, however, only a flush quantity P is drawn off. Further liquid is withdrawn from the first column 1 in the form of a stream d above the sump in liquid form and initially through a
  • Components remaining liquid in the evaporation chambers of the top condensers 141 and 161 are fed into the third column 13 and the second column 12 in the form of the streams e and f.
  • the stream f is conveyed back to the second column 12 by means of a pump 16.
  • gas formed in the evaporation chambers of the top condensers 141 and 151 is heated in the form of a collective flow g in the subcooling countercurrent 18 and then in the main heat exchanger 4.
  • the material flow g is then in a compressor 6 or a compressor stage, which or which in particular form a structural unit with a further compressor 7 or a further compressor stage can, in particular a combination compressor, compressed.
  • an after-cooler (not specifically designated) downstream of the compressor 6 or the compressor stage, the material flow g is cooled again in the main heat exchanger 4 and fed into the second column 12.
  • top gas of the first column 11 is cooled and returned in condensed form to the first column.
  • Overhead gas that has not been appropriately cooled is first heated in the form of a stream h in the subcooling countercurrent 18 and then in the main heat exchanger 4 and is carried out as part of a pressurized nitrogen product.
  • the bottom liquid of the second column 12 is withdrawn from this in the form of a stream i, passed through the subcooling countercurrent 18, heated in the second condenser evaporator 121 against top gas of the second column 12, again passed through the subcooling countercurrent 18, heated in the main heat exchanger 4 and after another Heating used as a regeneration gas in the adsorber unit 3 and / or released to the atmosphere A.
  • Condenser evaporator 131 is cooled and condensed in the third column 13 and returned to the second column 12 by means of a pump 17. More overhead gas is in the form of a stream I in the subcooling countercurrent 18 and in
  • Main heat exchanger 4 heated, compressed by means of the compressor 7, and used together with the material flow h to provide the pressurized nitrogen product.
  • a liquid side stream m is transferred from the second column 12 into the third column 13.
  • Bottom liquid of the third column 13 is withdrawn in the form of a stream n and after optional intermediate storage in a tank system T and after an optional, not shown internal compression in the
  • Main heat exchanger 4 heated and provided as an oxygen pressure product.
  • Oxygen-rich gas is drawn off from the third column 13 above the bottom in the form of a stream o.
  • This material flow o which is not illustrated further, can be heated and, for example, in subcooler 18 and main heat exchanger 4
  • Overhead gas withdrawn from the top of the third column 13 is heated in the form of a stream p in the subcooling countercurrent 18 and then in the main heat exchanger 4 and discharged as a low-pressure nitrogen product.
  • a gaseous, argon-enriched side stream q is withdrawn from the third column 13 and fed into the fourth column 14, that is to say the crude argon column.
  • Bottom liquid from the fourth column 14 is conveyed back into the third column 13 in the form of a stream r by means of the pump 19.
  • a non-condensed, argon-rich top gas from the fourth column 14 is transferred into the pure argon column 16 in the form of a stream s.
  • argon-rich liquid is carried out as an argon product in the form of a stream t.
  • This material flow t can also be subjected to an internal compression of a type known per se.
  • Gas withdrawn from the top of the pure argon column 16 can be released into atmosphere A, for example, in the form of a stream u.
  • the air separation plant 1002 illustrated in FIG. 2 differs from the air separation plant 1001 illustrated in FIG. 1 in that the
  • Condenser-evaporator 121 is designed as a bath condenser above the second column 12, in which a heat exchanger block 121a is submerged in a liquid bath which is formed by the material flow i. A flushing amount P is also deducted from this.
  • the air separation plant 1003 illustrated in FIG. 3 differs from the air separation plant 1001 illustrated in FIG. 1 in that the uppermost separating section 12a of the second column 12, which is shown here, is reduced in size and a corresponding additional separating section 13a, which is explicitly shown here, is provided in the third column 13 .
  • the stream f is correspondingly fed into the second column 12 and into the third column 13 in the form of two substreams f and f ′′.
  • the air separation plant 1004 illustrated in FIG. 4 differs from the air separation plant 1003 illustrated in FIG. 3 in that, in addition to the
  • the air separation plant 1005 illustrated in FIG. 5 differs from the air separation plant 1001 illustrated in FIG. 1 in that, in addition to the stream g not being heated, compressed and cooled as previously explained, before it is fed into the second column 12, but that this treatment is performed Substance flow g ′′ withdrawn from the third column 13 is subjected. The substance flow g, on the other hand, is fed directly into the second column 12. In this way, the volume flow of circulated gas can be increased or decreased.
  • the air separation plant 1006 illustrated in FIG. 6 differs from the air separation plant 1001 illustrated in FIG. 1 in that the material flow I is not compressed as explained above. Correspondingly, the compressor or the compressor stage 7 is also missing, and only the compressor 6 is present.
  • Compressed nitrogen product is here essentially formed by the correspondingly used top gas of the first column 11.
  • the low-pressure nitrogen of the stream I can be used, for example, as a sealing gas.
  • the air separation plant 1007 illustrated in FIG. 7 differs from the air separation plant 1001 illustrated in FIG. 1 in that a
  • High purity oxygen column formed further column 20 is present. This has an upper column part 21 and a lower column part 21.
  • the upper column part 21 of the further column 20 represents a part of the fourth column 14.
  • This column part is fed with a material flow q ′ corresponding to the material flow q explained above.
  • Liquid from the upper column part 21 is returned to the third column 13 in the form of a stream r '.
  • Top gas of the upper and lower column parts 21, 22 is combined and fed into the fourth column 14 in the form of a stream q ′′.
  • Bottom liquid from the fourth column 14 is in the form of a
  • An oxygen-rich stream n ' is withdrawn from the bottom of the second column part 22 and, like the stream n, is stored in a tank system T', possibly one Subject to internal compression, and can be run from the air separation unit 1007.
  • a bottom evaporator 23 of the further column 20 is heated with a substream b ′ of the feed air flow b, which can then be fed into the second column 12 and the third column 13 at the points marked b ′.
  • the air separation plant 1008 illustrated in FIG. 8 differs from the air separation plant 1007 illustrated in FIG. 7 in that a different one
  • Heating medium in the bottom evaporator 23 of the further column 20 is used.
  • the material flow k is divided here into partial flows k ′ and k ′′, the partial flow k ′ being passed through the third condenser evaporator 131 and the partial flow k ′′ being passed through the bottom evaporator 23.
  • the substreams k 'and k are then combined again and treated as before the stream k.
  • the air separation plant 1009 illustrated in FIG. 9 is shown in the drawing
  • the main heat exchanger 4 in a turbine arrangement 30, for example with an oil-braked turbine, is expanded before it is fed into the third condenser evaporator 131 and then into the second column 12.
  • Another side stream w from the first column 11 is fed directly into the third column 13.
  • Top condenser 141 of the fourth column 15 can be used as a coolant. Gas from the top condenser 141 can on the one hand be fed into the third column 13 and on the other hand with further material flows from the third column 13 or liquid from the second condenser-evaporator 121, which is used here as a bath evaporator is trained to be united. A material flow x formed in this way is heated in the main heat exchanger 4 and can, for example, be released into the atmosphere. Liquid from the top condenser 141 is fed into the third column 13 here. Further portions of the stream d 'can be fed directly into the third column 13, transferred as a coolant to the second condenser evaporator 121 and combined with the stream i.
  • Top gas of the second column 12 is formed in the second condenser-evaporator 121, returned to the first column 11 in the form of a stream y, and streams z are transferred from the second column 12 to the third column 13.
  • the material flow i is heated and expanded in a turbine arrangement 40, for example with an oil-braked turbine.
  • This relaxed stream or a portion thereof, denoted here by i ′′, can be used as residual gas to regenerate the adsorber unit 3; an optional further proportion, denoted here by i ′ ′′, is fed into the third column 13.
  • a stream t ′ from the fourth column can be used as an argon product or transferred to a pure argon column 16.
  • the material flow p can optionally be compressed and used accordingly.
  • several subcoolers 50 are illustrated, but also to several, in particular in one
  • Subcooling countercurrent 18 as before can be combined. Hypothermia can also occur in other places.
  • the air separation plant 1010 illustrated in FIG. 10 differs from the air separation plant 1009 illustrated in FIG. 10 in that a further column 15, here referred to as the “fifth” column, is present. This is fed with the expanded feed air stream c, and it is designed with the third column 13 as a double column. Overhead gas of the fifth column 15 is liquefied in the third condenser-evaporator 131 and returned to the fifth column 15.
  • the material flow v can, but does not have to be present. In the latter case, an embodiment of the air separation plant 1010 that is not according to the invention is implemented. Gas can be transferred from the fifth column 15 to the first column 11 in the form of a stream z ′.
  • the material flow d ' is not formed, instead a
  • the air separation plant 1011 shown in FIG. 11 differs from the air separation plant 1009 shown in FIG. 10 in that, instead of the material flow i ', the material flow x is used as regeneration gas in the adsorber unit 3 and the material flow i' is released into the atmosphere instead.

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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)

Abstract

L'invention concerne un procédé pour la décomposition d'air à basse température, dans lequel une installation de décomposition d'air (1001-1011) comprenant un système de colonnes (10) est utilisée, laquelle comprend une première colonne (11), une deuxième colonne (12), une troisième colonne (13) et une quatrième colonne (14), la première colonne (11) fonctionnant dans une première plage de pression, la deuxième colonne (12) fonctionnant dans une deuxième plage de pression inférieure à la première plage de pression et la troisième colonne (13) et la quatrième colonne (14) fonctionnant dans une troisième plage de pression inférieure à la deuxième plage de pression, du fluide étant injecté dans la deuxième colonne (12) à partir de la première colonne (11), du fluide étant injecté dans la troisième colonne (13) à partir de la deuxième colonne (12) et du fluide étant injecté dans la quatrième colonne (14) à partir de la troisième colonne (13), le fluide injecté dans la quatrième colonne (14) à partir de la troisième colonne (13) comprenant au mois une partie du soutirage latéral soutiré de la troisième colonne (13). Du gaz de tête de la première colonne (11) est soumis à une condensation contre du liquide de puits de la deuxième colonne (12) et retourné à l'état liquide à la première colonne (11) et du liquide de puits de la troisième colonne (13) est évacué de l'installation de décomposition d'air (1001-1011) comme produit riche en oxygène. Selon l'invention, le gaz de tête de la deuxième colonne (12) est soumis à une condensation contre un autre liquide de puits de la deuxième colonne (12) et retourné à l'état liquide à la deuxième colonne (12), et un autre gaz de tête de la deuxième colonne (12) ou un gaz différent de la première colonne (11) ou de la deuxième colonne (12) est soumis à une condensation contre un autre liquide de puits de la troisième colonne (12) et retourné à la deuxième colonne (12). La présente invention concerne également une installation de décomposition d'air (1001-1011) correspondante.
PCT/EP2020/025125 2019-03-15 2020-03-12 Procédé et installation de décomposition d'air à basse température WO2020187449A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021190784A1 (fr) * 2020-03-23 2021-09-30 Linde Gmbh Procédé et installation de séparation d'air à basse température

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US3079759A (en) * 1961-03-22 1963-03-05 Air Prod & Chem Separation of gaseous mixtures
EP0694744A1 (fr) * 1994-07-25 1996-01-31 The BOC Group plc Séparation de l'air
EP0752565A2 (fr) * 1995-07-06 1997-01-08 The BOC Group plc Production d'argon
EP1227288A1 (fr) 2001-01-30 2002-07-31 Linde Aktiengesellschaft Système à trois colonnes pour la séparation cryogénique de l'air

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US3079759A (en) * 1961-03-22 1963-03-05 Air Prod & Chem Separation of gaseous mixtures
EP0694744A1 (fr) * 1994-07-25 1996-01-31 The BOC Group plc Séparation de l'air
EP0752565A2 (fr) * 1995-07-06 1997-01-08 The BOC Group plc Production d'argon
EP1227288A1 (fr) 2001-01-30 2002-07-31 Linde Aktiengesellschaft Système à trois colonnes pour la séparation cryogénique de l'air

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Title
"Industrial Gases Processing", 2006, WILEY-VCH

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021190784A1 (fr) * 2020-03-23 2021-09-30 Linde Gmbh Procédé et installation de séparation d'air à basse température

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