EP3101374A2 - Procede et installation cryogeniques de separation d'air - Google Patents

Procede et installation cryogeniques de separation d'air Download PDF

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Publication number
EP3101374A2
EP3101374A2 EP16001082.3A EP16001082A EP3101374A2 EP 3101374 A2 EP3101374 A2 EP 3101374A2 EP 16001082 A EP16001082 A EP 16001082A EP 3101374 A2 EP3101374 A2 EP 3101374A2
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Prior art keywords
air
pressure level
gear
pressure
partial
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EP16001082.3A
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German (de)
English (en)
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EP3101374A3 (fr
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Dimitri Goloubev
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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
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • 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
    • F25J3/04024—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 purified feed air, so-called boosted air
    • 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
    • F25J3/04036—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 oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—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
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    • F25J3/04042—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 argon or argon enriched stream
    • 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
    • F25J3/04006—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
    • F25J3/04054—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 air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel

Definitions

  • the invention relates to a method and a plant for the cryogenic separation of air according to the preambles of the independent claims.
  • cryogenic separation of air in air separation plants is known and, for example at H.-W. Haring (ed.), Industrial Gases Processing, Wiley-VCH, 2006, especially Section 2.2.5, "Cryogenic Rectification
  • the present invention is particularly suitable for air separation plants with internal compression, as described above, Section 2.2.5.2, “Internal Compression” explained.
  • Air separation plants have distillation column systems which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three-column or multi-column systems.
  • distillation columns for the recovery of nitrogen and / or oxygen in the liquid and / or gaseous state for example, liquid oxygen, LOX, gaseous oxygen, GOX, liquid nitrogen, LIN and / or gaseous nitrogen, GAN
  • distillation columns for nitrogen-oxygen Separation distillation columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
  • the distillation column systems of air separation plants are operated at different operating pressures in their distillation columns.
  • Known double column systems have, for example, a so-called (high) pressure column and a so-called low-pressure column.
  • the operating pressure of the high-pressure column is, for example, 4.3 to 6.9 bar, in particular about 5.5 bar.
  • the low-pressure column is operated at an operating pressure of, for example, 1.2 to 1.7 bar, in particular about 1.4 bar.
  • the pressures given here are absolute pressures in the bottom of corresponding distillation columns.
  • the pressures mentioned below are also referred to as "distillation pressures", because in them the fractional distillation the respectively fed air takes place within the distillation columns. This does not exclude that other pressures may be present elsewhere in a distillation column system.
  • feed air cooled compressed air
  • compressors for example, main air compressors and booster
  • Products obtained in a corresponding air separation plant can also be pressurized with compressors (product compressors) or corresponding combinations of compressors.
  • the operating costs (OPEX) of an air separation plant are mainly determined by energy consumption, which in turn depends mainly on the energy consumption of the compressors (main air compressors, booster and product compressor, if any).
  • the investment costs (CAPEX) are also significantly determined by the cost of providing the compressors.
  • MAC International Main Air Compressor
  • BAC booster compressor
  • HAP High Air Pressure
  • the total feed air is compressed in a main air compressor to a pressure that is well above the distillation pressure in the high pressure column.
  • the pressure difference used is at least 4 bar and preferably between 6 and 16 bar.
  • HAP methods are for example from EP 2 466 236 A1 , of the EP 2 458 311 A1 and the US 5,329,776 A known, MAC / BAC method, for example, from the literature cited above.
  • the US 5 901 579A shows a coupled via a gearbox turbo compressor and turboexpander for use in a HAP process. From the EP 2 634 517 A1 and the EP 2 520 886 A1 Arrangements are known in which so-called cold compressors or cold booster (see below) are used.
  • Air separation plants can, as mentioned, be operated with so-called internal compression.
  • the internal compression for example, to provide the above-mentioned gaseous, internally compressed oxygen pressure, a liquid stream is removed from the distillation column system and at least partially brought to liquid pressure. The liquid brought to pressure is heated in a main heat exchanger of the air separation plant against a heat transfer medium and evaporated.
  • the liquid stream may in particular be liquid oxygen, but also nitrogen or argon.
  • the internal compression is thus used to obtain appropriate gaseous printed products.
  • the advantage of internal compression processes is that corresponding fluids do not have to be compressed outside the air separation plant in a gaseous state, which often proves to be very complicated and / or requires expensive safety measures.
  • the term "evaporation” includes, as also explained below, in the internal compression cases in which there is a supercritical pressure and therefore no phase transition takes place in the true sense.
  • the liquid pressurized stream is then "pseudo-evaporated".
  • a heat transfer medium is liquefied (or pseudo-liquefied if it is under supercritical pressure) against a (pseudo) vaporising stream.
  • the heat carrier is usually formed by a partial flow of the compressed feed air, which is referred to as inductor current.
  • inductor current In a warmer area of the used in the evaporation or pseudo-vaporization Heat exchanger can be introduced additional heat of vaporization by the so-called turbine flow (or by multiple turbine streams).
  • this heat transfer medium In order to efficiently heat and vaporize the stream brought to liquid pressure, this heat transfer medium must have a relatively high pressure due to thermodynamic conditions. Therefore, a correspondingly high-density power must be provided. If, for example, for use in the aforementioned CTX method or the gasification of heavy oil, but also in other scenarios, internally compressed pressure oxygen with high or very high pressures (for example, 50 bar and more) are provided, this is particularly true.
  • the present invention therefore has as its object to provide possibilities that allow to carry out a corresponding compression in a simple and efficient manner in a HAP process.
  • the present invention proposes a method and an installation for the cryogenic separation of air with the features of the independent claims.
  • Embodiments are each the subject of the dependent claims and the following description.
  • turbo compressors are used to compress the air. This applies, for example, to the “main (air) compressor”, which is characterized by the fact that through this the total amount of air fed into the air separation plant, ie the entire "feed air", is compressed.
  • additional turbo compressors are provided, which are also referred to as boosters.
  • turboexpander can be used. This applies in particular to the relaxation of a so-called turbine flow, as explained below.
  • Turboexpanders can also be coupled with turbo compressors (boosters) and drive them. If one or more turbocompressors without externally supplied energy, i. driven only by one or more turboexpander, the term "turbine booster" is used for such an arrangement.
  • turbocompressors and turboexpanders The mechanical structure of turbocompressors and turboexpanders is known to those skilled in principle.
  • a turbo compressor the compression of the air by means of blades, which are arranged on an impeller or directly on a shaft, a turbo-compressor forms a structural unit, however, which may have a plurality of "compressor stages".
  • a compressor stage typically includes an impeller or a corresponding array of blades. All of these compressor stages can be driven by a common shaft.
  • a turboexpander is basically designed to be comparable, but the blades are driven by the expanding air. Again, several expansion stages can be provided.
  • Turbo compressor and turboexpander can be designed as radial or axial machines.
  • the blades of a turbocompressor or turboexpander are “non-rotatably coupled” with another element, such as a drive wheel or output gear, this means that there is a mechanical connection between the blades and the other element.
  • the blades are, as mentioned, attached to one or more impellers or rotatably connected to a shaft, or directly to a shaft, so that a direct torque transmission between the shaft and blades is possible. In this way, each rotatably coupled to the shaft member is also rotatably coupled to the blades.
  • Such a “rotationally fixed coupling” causes a rotational speed equal and the same direction of rotation of the blades and the other element, such as the drive wheel or the driven wheel, about the axis of the Wave.
  • a coupling across a gear engagement is not a “non-rotatable coupling” in the sense explained.
  • a “drive wheel” is understood below to mean a gear which is acted on by a shaft with a torque, in particular by being coupled to the rotor blades of a turboexpander.
  • a “driven wheel” is a toothed wheel which in turn applies a torque to a shaft, in particular the shaft of a turbocompressor.
  • pressure level and "temperature level” to characterize pressures and temperatures, thereby indicating that corresponding pressures and temperatures need not be used in the form of exact pressure and temperature values, respectively, to the inventive concept realize.
  • pressures and temperatures typically range in certain ranges that are, for example, ⁇ 1%, 5%, 10%, 20% or even 50% about an average.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another. In particular, for example, pressure levels include unavoidable or expected pressure drops. The same applies to temperature levels.
  • the pressure levels indicated here in bar are absolute pressures.
  • a cold booster is understood to mean a turbocompressor which is charged with air at low temperatures, generally below 0 ° C. This is advantageously driven by means of a turboexpander.
  • a single stage compression of said current is merely a hypothetical example for illustration in the accompanying drawings FIG. 1 shown.
  • a single-stage compression is not sufficient to achieve the required pressures, since the achievable pressure ratio of the cold booster is limited (the pressure ratio ⁇ in corresponding turbocompressors is usually not higher than 1.8 to 2.0).
  • the flow rate of the correspondingly high air flow to be compressed in an energy-optimized design, a second air flow is used at a lower pressure level) is much lower than the mass flow of the air, which is expanded in a usable for driving turboexpander. This would lead to very different specific speeds, which is why a corresponding unit is currently not buildable.
  • this problem could be circumvented by using a two-stage arrangement instead of a single-stage cold booster which is at least partially driven externally, for example by electrical energy.
  • this is not desirable as a rule, since this would cause additional costs both by the required provision of an electric motor and by the dimensioning of the local medium-voltage network.
  • HAP methods can, as explained below, manage completely without the use of electric motors for compression, so that the provision of an electric motor and the required infrastructure would be particularly disadvantageous here.
  • FIG. 2 Another arrangement, also for purposes of illustration only, is FIG. 2 shown and explained below.
  • a corresponding arrangement has not been considered in the cold part of a corresponding system so far, but is known per se and has already been used in "warm” turbine booster, if there are very different flow rates.
  • the ratios of the volumetric flows remained too unbalanced, so that such a unit because of too different specific speeds currently also not buildable.
  • the amount of inductor current would have to be increased and the amount of turbine flow reduced. As a result, however, the method loses efficiency because the final pressure of the throttle current would be lower.
  • the present invention was therefore based on the search for an arrangement which allows a two-stage compression of the throttle flow at optimum proportions by means of a turbine drive.
  • a compression / expansion arrangement in which several (ie two or more) driving turboexpanders are connected in parallel and two or more turbo compressors are connected in series, solves the problems explained above.
  • an intermediate transmission is used as explained below in the context of the invention.
  • the use of such an intermediate gear allows the decoupling of specific speeds and allows the desired drive.
  • the inventively proposed arrangement is similar to a so-called Compander, in which a turbo compressor is coupled with a turboexpander via an intermediate gear. According to the invention, however, neither a generator nor an engine are needed.
  • the present invention proposes a process for the distillative cryogenic separation of feed air in a distillation column system of an air separation plant at different distillation pressures.
  • the total feed air is compressed in a total amount of air to a first pressure level, which is at least 4 to 5 bar above the highest of the distillation pressures.
  • a first pressure level which is at least 4 to 5 bar above the highest of the distillation pressures.
  • an HAP method explained at the outset is used.
  • the total feed air is compressed to a pressure level which is at least 4 to 5 bar above such pressure, that is, for example at least 11, 12, 13, 14, 15 or 16 bar. Specific values are explained below.
  • a first partial air quantity of the mentioned total air quantity is first cooled to a first temperature level of 130 to 170 K, typically in a main heat exchanger of a corresponding air separation plant, and then compressed to a second pressure level which is at least 10 bar above the first pressure level ,
  • the present invention is thus used in HAP processes in which comparatively high pressures are generated, for example in order to be able to provide internally compressed printed products at correspondingly high pressures, as explained below.
  • a second partial air quantity is first cooled to a second temperature level of 110 to 150 K and then released to a third pressure level which is below the first pressure level and, for example, at the highest of the distillation pressures, ie the operating pressure of the high pressure column can.
  • the cooling to the second temperature level can also be done in a main heat exchanger of the air separation plant.
  • the present invention contemplates using a compression / expansion assembly with a transmission in which a drive wheel is engaged with a gear and the gear is engaged with a driven gear.
  • a drive wheel With the drive wheel, the blades of two or more turboexpander and the driven wheel, the blades of two or more turbocompressors in the above-described sense are rotatably coupled.
  • the first partial air quantity is performed for compression to the second pressure level in succession by the turbo-compressor and the second partial air volume for relaxation to the third pressure level in parallel through the turboexpander.
  • a "parallel" guiding by a plurality of turboexpanders is understood to mean that the second partial air quantity is divided into two or more partial flows and each of the partial flows is guided through one of the turboexpanders.
  • the speeds of each turbo compressor and turboexpander used are adapted to each other.
  • very high pressure differences can be generated, which would not be achieved with only one compressor unit.
  • the invention also allows the use of first and second partial air quantities in significantly different orders of magnitude, since the use of the transmission speed differences can be compensated.
  • the guided through the turbo compressor first partial air amount is present at the first temperature level explained. Therefore, the turbocompressors are operated as a cold booster.
  • turboexpanders are connected in parallel in the context of the present invention, the mechanical loads that occur can be distributed symmetrically and the individual turboexpanders can be made smaller and less expensive.
  • the blades are coupled on both sides of the driven gear each with a driven shaft coupled to the first shaft. In this way, asymmetric loads can be reduced and wear reduced.
  • a torque transmitted to the gear wheel by means of the drive wheel is greater than or equal to a torque transmitted to the output gear by means of the gear wheel. So there is no need to provide additional drives such as an electric motor, the turbocompressors can only be driven by the turboexpander.
  • a further advantage of the compression / expansion arrangement according to the invention is that flexible additional driving or driven gears can be brought into engagement with the gear wheel and therefore the method can be expanded as desired.
  • one or more further turboexpanders driving via a drive wheel and / or one or more turbo compressors driven by the turbine wheel via a driven wheel can be used.
  • the gear itself is preferably not rotatably coupled with turbo expanders and / or turbo compressors, but preferably transmits only torques between drive and driven wheels.
  • the gear on the one hand and the driving or driven units on the other hand for example, the blades of turboexpanders and turbocompressors
  • the driving or driven units on the other hand for example, the blades of turboexpanders and turbocompressors
  • the driving or driven units can be operated with equal speed to each other.
  • the second pressure level is thus at comparatively high values, which make the use of a single booster no longer possible, since in this, as explained, the achievable pressure difference is too low.
  • the third pressure level which is below the first pressure level, may, for example, be at the highest of the distillation pressures in the distillation column arrangement, for example the pressure level at which a high pressure column is operated.
  • the third pressure level is "at” the highest of the distillation pressures, it is meant that the third pressure level does not deviate by more than 1 bar from the highest of the distillation pressures of the distillation column arrangement.
  • the present invention is particularly suitable when the respective partial air volumes differ significantly from one another. This is the case in particular if the first partial air quantity corresponds to 0.2 times to 0.6 times the second partial air quantity and / or if the first and the second partial air quantities together are 0.3 times to 0.6 times correspond to the total amount of air.
  • the ratios mentioned relate in each case to standard volumes per unit time, ie standard volume flows, for example standard cubic meters per hour (Nm 3 / h).
  • standard volume flows for example standard cubic meters per hour (Nm 3 / h).
  • the differences in the actual volumetric flows present are much higher because there are widely differing pressures.
  • the method of the present invention is due to the use of the illustrated transmission.
  • the second partial air quantity before cooling to the second temperature level is compressed from the first pressure level to an intermediate pressure level which is below the second pressure level.
  • another turbo-compressor can be used. This can be powered by a (for the purpose of providing the necessary cooling capacity for the entire process) turboexpander, which relaxes another stream.
  • the process of the invention develops particular advantages when the distillation column system is taken from a liquid, oxygen-rich air product, increased in pressure and then transferred by heating from the liquid to the supercritical or gaseous state, ie for internal compression processes.
  • the liquid, oxygen-rich air product can be liquid-pressure-elevated to the first pressure level or another high pressure level.
  • the invention is therefore particularly suitable for processes in which corresponding internal compression products are to be provided at high pressures.
  • the air compressors are typically driven by steam turbines.
  • the steam turbines used in this case are typically twin-shaft turbines, which are set up for the simultaneous drive of main and secondary compressors (MAC and BAC in MAC / BAC method) by means of one of the shafts in each case.
  • a typically additionally required nitrogen product compressor requires its own drive in the form of an electric motor in a MAC / BAC method. This causes additional costs, as explained above. Therefore, HAP methods are particularly advantageous because here the product compressor can be driven directly via one of the shafts of the steam turbine (the booster falls away). Such systems therefore benefit particularly from solutions that do not require electric drives.
  • the present invention further relates to an air separation plant, which is set up for the distillative cryogenic separation of feed air in a distillation column system at different distillation pressures.
  • This plant has means which are adapted to compress the total feed air in a total amount of air to a first pressure level which is at least 4 to 5 bar above the highest of the distillation pressures, from the total amount of air a first partial air amount initially to a first temperature level of 130 to cool to 170 K and thereafter to compress to a second pressure level which is at least 10 bar above the first pressure level, and to first cool a second partial air volume to a second temperature level of 110 to 150 K and thereafter to relax to a third temperature level below that first pressure levels.
  • the system is characterized by a compression / expansion arrangement with a transmission, in which according to the invention a drive wheel with a gear and the gear is in engagement with a driven gear.
  • a drive wheel with a gear and the gear is in engagement with a driven gear.
  • the blades of two or more turboexpander and the driven wheel With the drive wheel, the blades of two or more turboexpander and the driven wheel, the blades of two or more turbo compressors are coupled.
  • Means are provided which are adapted to lead the first partial air quantity for compression to the second pressure level in succession through the turbo-compressor and the second partial air volume for expansion to the third pressure level in parallel through the turboexpanders.
  • an arrangement is used in the context of the present invention, in which at least one further drive wheel and / or at least one further output gear is in engagement with the gear wheel.
  • further driving or driven units can be coupled with a corresponding compression / expansion arrangement in a simple and flexible manner.
  • the present invention is suitable for air separation plants, in which the compression / expansion arrangement comprises two turbocompressors, the blades are coupled on both sides of the driven gear with a driven shaft coupled to the first shaft, and / or two turboexpander, the blades on both sides of the drive wheel with a coupled to the drive wheel coupled second shaft.
  • the compression / expansion arrangement comprises two turbocompressors
  • the blades are coupled on both sides of the driven gear with a driven shaft coupled to the first shaft
  • / or two turboexpander the blades on both sides of the drive wheel with a coupled to the drive wheel coupled second shaft.
  • FIG. 1 an air separation plant for illustrating the underlying object of the invention in the form of a schematic process flow diagram is illustrated and designated 100 in total.
  • the air separation plant 100 is fed via a filter 1 feed air (AIR), which is compressed by means of a main air compressor 2.
  • AIR filter 1 feed air
  • the compression of the feed air in the main air compressor 2 takes place at pressure level, which is referred to in this application as "first" pressure level and which is significantly higher than the maximum operating pressure of a below explained distillation column system 10 of the air separation plant 100.
  • the process performed in the air separation plant 100 So is a HAP method as explained above.
  • the first pressure level is for example about 14.5 bar.
  • the compressed by the main air compressor 2 amount of air flow c is referred to here as "total air amount”. This is, for example, about 655,000 Nm 3 / h.
  • a compressed air flow a provided in this way is precooled in a direct contact cooler 3, which is charged inter alia with a cooled water flow b from an evaporative cooler 4.
  • the operation of the direct contact cooler 3 and the evaporative cooler 4 will not be explained in detail.
  • a correspondingly cooled compressed air flow now denoted by c, is fed to an adsorber 5, which in the illustrated example comprises two adsorber vessels filled with a suitable adsorption material and operated in alternating operation and whose operation is likewise not explained in detail.
  • evaporative cooler 4 and the Adsorbersatz 5 can be used for cooling or regeneration, for example, a stream d, which is taken from the distillation column system 10 as a so-called impure nitrogen and processed in a suitable manner.
  • a steam heater 6 is used.
  • a dried in the Adsorbersatz 5 compressed air flow is denoted by d. This is divided in the example shown in two sub-streams e and f.
  • the partial flow e is then divided again into two partial flows g and h and fed to a main heat exchanger 7 on the hot side.
  • the partial flow g is the explained turbine flow
  • the partial flow h is a (second) throttle flow with lower pressure.
  • the partial flow f is further compressed in a booster turbine 8, cooled in a not separately designated aftercooler, split again into two partial flows i and k and fed to the main heat exchanger 8 on the hot side.
  • the partial flow i is a higher pressure (first) throttle flow to be compressed
  • the partial flow k is a flow to be expanded to provide cooling power.
  • All sub-streams e to k thus each comprise partial air quantities of the total air quantity of the stream a, c or d.
  • the partial air quantity encompassed by stream i for example approx. 102,000 Nm 3 / h, is referred to here as the "first" partial air quantity
  • the partial air quantity comprised by stream g for example approx. 307,000 Nm 3 / h
  • the partial air volume of the total amount of air comprised by stream h is, for example, approximately 55,000 Nm 3 / h.
  • the division is arbitrary and can, in deviation from the specific example, also be carried out in a different order.
  • the partial flows g, i and k are taken from the main heat exchanger 7 respectively to intermediate temperature levels, the intermediate temperature level at which the partial flow i is taken from the main heat exchanger 7, taken here as the "first" temperature level and the intermediate temperature level at which the partial flow g from the main heat exchanger 7 is referred to as the "second" temperature level.
  • the partial flow h is removed from the main heat exchanger 7 cold side.
  • air separation plant is to provide internally compressed pressure oxygen at a high pressure level, for example, to about 57 bar, and set in an amount of, for example, about 135,000 Nm 3 / h.
  • a liquid, oxygen-rich stream I is removed, increased pressure by means of a pump 9 and transferred in the Hautpsagen (2004)er 7 from the liquid to the supercritical state at the mentioned pressure.
  • the partial flow i would have to be compressed after removal from the main heat exchanger 7 at the first intermediate temperature level by means of the booster turbine 101, starting from the achieved in the booster turbine 8 pressure level of, for example, about 17 bar to a pressure level of, for example, about 57 bar.
  • a corresponding pressure level is referred to herein as a "second" pressure level.
  • the partial flow i is fed to the main heat exchanger 7 at an intermediate temperature level and removed from it on the cold side.
  • the partial flows h and i are in the example shown downstream of the main heat exchanger 7 to a lower pressure level, for example, the pressure level of a pressure column in the distillation column assembly 10 of about 5.2 bar, relaxed.
  • a pressure level can also take place for the partial flows g and k in the respective expansion turbines of the booster turbines 8 and 101, respectively.
  • the partial streams g to k are fed into the distillation column system 10 mentioned a number of times, which here is represented in a highly schematized and miniaturized manner and typically comprises a plurality of distillation columns operated at different operating pressures.
  • a high-pressure column 11 and a low-pressure column 12 are shown, which are in heat exchanging connection via a main capacitor 13.
  • the high-pressure column 11 is operated, for example, at the pressure level to which the currents g to k are relaxed.
  • the streams g to k are typically fed into the high pressure column 11, but it can also be partially fed into the low pressure column 12.
  • the interconnection of the high-pressure column 11 and the low-pressure column 12 is not shown in detail, as well as additional columns, valves, pumps, heat exchangers and the like.
  • the distillation column system 10 may comprise any number of corresponding columns and may be configured to recover different products of air.
  • the distillation column system 10 for example, a nitrogen-rich, liquid stream m can be removed, which also by means of a pump (without reference numerals) pressure-increased and in the main heat exchanger 7 in gaseous or supercritical state can be transferred.
  • Further nitrogen-rich streams n and o can be taken from the high-pressure column 11, for example in gaseous form, heated in the main heat exchanger 7 and used as gaseous nitrogen product (GAN) or sealing gas for pumps (seal gas).
  • GAN gaseous nitrogen product
  • sealing gas for pumps
  • FIG. 2 an air separation plant to illustrate the underlying task of the invention in the form of a schematic process flow diagram is illustrated and indicated generally at 200.
  • FIG. 2 illustrated air separation plant 200, which incidentally the in FIG. 1 illustrated air separation plant 100, it is explained that even a use of serial booster or parallel turboexpander alone does not solve the problems explained above or is not technically feasible.
  • the partial flow i in the boosters of two booster turbines 201 and 202 would be compressed via an intermediate pressure level of, for example, about 31 bar to the previously described second pressure level of, for example, about 57 bar.
  • the partial flow i can, as in FIG. 2 not illustrated, after exiting the boosters of the booster turbine 201 and before entering the boosters of the booster turbine 202, for example, are cooled in the main heat exchanger 7, so that its inlet temperature in the boosters of the booster turbines 201 and 202 is the same or similar.
  • the partial flow g would be divided into two partial flows and expanded in the turboexpanders assigned to the booster turbines 201 and 202.
  • the turboexpander would only have to process half of the "second" partial air quantity of the stream g, ie in the example shown, in each case, for example, about 153,000 Nm 3 / h. Nevertheless, the volume flow through the booster of the booster turbine 202 would still be too small for the volume flow through the corresponding turboexpander and thus the specific speeds are too different, so that this solution is also not feasible.
  • FIG. 3 a compression / deflation arrangement according to an embodiment of the invention is schematically illustrated and indicated generally at 30.
  • the integration results from the corresponding designation of the partial flows g and i. These are in each case the streams g and i downstream of the main heat exchanger 7.
  • the mentioned first partial air quantity of the total amount of air as mentioned, for example, about 102,000 Nm 3 / h at a pressure level of about 17 bar, in the form of the partial flow i is successively guided by two turbo compressors 31 and 32 and thereby to the mentioned second pressure level of for example approx 57 bar compressed.
  • the pressure of the partial flow i between the turbocompressors 31 and 32 is for example about 31 bar.
  • a cooling of the current i in the main heat exchanger 7 or otherwise take place.
  • the second partial air amount of the total amount of air is divided in the form of the partial flow g on two partial streams and relaxed in parallel in two turboexpanders 33 and 34, as mentioned for example, about 5.2 bar.
  • the turbocompressors 31 and 32 and the turboexpanders 33 and 34 are connected to each other via shafts 35 and 36, respectively.
  • a driven gear 37 is mounted on the shaft 37 of the turboexpander 33 and 34, a drive wheel 38. Both with the driven gear 37 and the drive wheel 38 is a gear 39 is engaged.
  • a torque introduced into the shaft 36 by the parallel relaxation of the partial flows of the flow g in the turboexpanders 33 and 34 can be introduced via the drive wheel 38 to the gear wheel 39 and from there via the output gear 37 into the shaft 35.
  • the gear 39 and the driven gear 37 can be ensured that, as mentioned, greatly different volume flows in the turboexpanders 31 and 32 on the one hand and in the turbocompressors 33 and 34 on the other hand copes easily can be.
  • FIG. 4 a compression / expansion arrangement not according to the invention is illustrated schematically and designated 40 as a whole.
  • Compression / expansion arrangement 40 can also be used instead of the booster turbine 101 or the booster turbines 201 and 202 in an air separation plant 100 or 200 in accordance with FIGS. 1 and 2 to be involved.
  • the integration also results here by the corresponding designation of the partial flows g and i. These are in each case the streams g and i downstream of the main heat exchanger 7.
EP16001082.3A 2015-06-03 2016-05-12 Procede et installation cryogeniques de separation d'air Withdrawn EP3101374A3 (fr)

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EP3935266A4 (fr) * 2019-03-06 2023-04-05 Industrom Power, LLC Système de récupération de chaleur perdue à cycle en cascade à refroidissement intermédiaire
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EP3410050A1 (fr) 2017-06-02 2018-12-05 Linde Aktiengesellschaft Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air
US11098950B2 (en) 2017-06-02 2021-08-24 Linde Aktiengesellschaft Process for obtaining one or more air products and air separation plant
RU2768445C2 (ru) * 2017-06-02 2022-03-24 Линде Акциенгезельшафт Способ получения одного или более продуктов из воздуха и установка по разделению воздуха
WO2019214847A1 (fr) 2018-05-07 2019-11-14 Linde Aktiengesellschaft Procédé pour produire un ou plusieurs produit(s) formés à partir d'air et installation de séparation d'air
WO2023051946A1 (fr) * 2021-09-29 2023-04-06 Linde Gmbh Procédé de séparation cryogénique de l'air et installation de séparation d'air

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CN106247758A (zh) 2016-12-21
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