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EP3699534A1 - Procédé et installation de séparation d'air permettant de fournir de manière variable un produit dérivé de l'air gazeux sous pression - Google Patents

Procédé et installation de séparation d'air permettant de fournir de manière variable un produit dérivé de l'air gazeux sous pression Download PDF

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Publication number
EP3699534A1
EP3699534A1 EP19020075.8A EP19020075A EP3699534A1 EP 3699534 A1 EP3699534 A1 EP 3699534A1 EP 19020075 A EP19020075 A EP 19020075A EP 3699534 A1 EP3699534 A1 EP 3699534A1
Authority
EP
European Patent Office
Prior art keywords
pressure
air
product
pump
gaseous
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP19020075.8A
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German (de)
English (en)
Inventor
Lars Kirchner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP19020075.8A priority Critical patent/EP3699534A1/fr
Publication of EP3699534A1 publication Critical patent/EP3699534A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04096—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
    • 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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the invention relates to a method for the variable provision of a gaseous, pressurized air product and a corresponding air separation plant according to the preambles of the independent claims.
  • air product is intended to refer to a fluid provided at least in part by the cryogenic decomposition of atmospheric air.
  • An air product has one or more air gases contained in atmospheric air in a composition that differs from that in atmospheric air.
  • An air product can basically be in a gaseous, liquid or supercritical state and can be transferred from one of these states to another.
  • a liquid air product can be converted into the gaseous state (“evaporated”) or converted into the supercritical state (“pseudo-evaporated”) by heating to a certain pressure, depending on whether the pressure during the heating is below or above the critical pressure .
  • Air separation plants have rectification column systems which are conventionally designed as two-column systems, in particular as classic Linde double-column systems, but can also be designed as three- or multi-column systems.
  • 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 thereof are used synonymously.
  • the rectification columns of the rectification column systems mentioned are operated at different pressures.
  • 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 of 4 to 7 bar, in particular about 5.3 bar.
  • the low-pressure column is operated at a pressure of typically 1 to 2 bar, in particular about 1.4 bar. In certain cases, higher pressures can also be used in both rectification columns.
  • the pressures given here are absolute pressures at the top of the columns given.
  • main (air) compressors / booster Main Air Compressor / Booster Air Compressor, MAC-BAC
  • HAP high air pressure
  • the main compressor / booster processes are the more conventional processes, while high-air pressure processes have been used more and more recently as alternatives.
  • the present invention is suitable for both variants of air separation. Because of their significantly lower costs and comparable efficiency, high-air pressure processes can represent an advantageous alternative to main compressor / booster processes.
  • Main compressor / booster processes are characterized in that only part of the total amount of feed air supplied to the rectification column system is compressed to a pressure which is significantly above, ie by at least 3, 4, 5, 6, 7, 8, 9 or 10 bar the pressure at which the high pressure column is operated. A further part of the feed air quantity is only compressed to this pressure or a pressure which differs therefrom by no more than 1 to 2 bar, and at this point it is fed into the high pressure column.
  • a main compressor / booster method is, for example, at Häring (see above) in Figure 2 .3A shown.
  • the entire amount of feed air supplied to the rectification column system is reduced to one pressure compressed, which is substantially, ie by at least 3, 4, 5, 6, 7, 8, 9 or 10 bar, and for example up to 14, 16, 18 or 20 bar, to above the pressure at which the high pressure column is operated .
  • High air pressure methods are, for example, from the EP 2 980 514 A1 and the EP 2 963 367 A1 known.
  • the present invention is used in air separation plants with so-called internal compression (IV, Internal Compression, IC).
  • at least one gaseous, pressurized air product which is provided by means of the air separation plant, is formed by removing a cryogenic, liquid air product from the rectification column system, subjecting it to a pressure increase to a product pressure, and heating it to the gaseous or supercritical state at the product pressure .
  • gaseous, pressurized oxygen GOX IV, GOX IC
  • gaseous, pressurized nitrogen GAN IV, GAN IC
  • GAR IV, GAR IC gaseous, pressurized argon
  • the internal compression offers a number of advantages compared to an alternatively also possible external compression and is explained, for example, by Häring (see above) in Section 2.2.5.2, "Internal Compression". Systems for the low-temperature separation of air, in which internal compression is used, are also in the US 2007/0209389 A1 and in the WO 2015/127648 A1 shown.
  • the present invention relates to the variable provision of corresponding gaseous, pressurized air products using internal compression, the term "variable” being intended in particular to refer to the amount in which a corresponding air product is made available per unit of time.
  • a corresponding provision in the sense understood here is variable in particular when the amount in which the air product is made available in a first period per unit of time is more than twice or 5 times and in particular up to 10 times the amount , in which the air product is provided in a second period per unit of time.
  • the present invention has the object of designing the variable provision of gaseous, pressurized air products by internal compression in a manner that is advantageous compared to the prior art.
  • the present invention proposes a method for the variable provision of a gaseous, pressurized air product and a corresponding air separation plant. Refinements are the subject of the dependent claims and the following description.
  • the present invention proposes a method for the variable production of a gaseous, pressurized air product, in which the air product is first formed in a liquid state using an air separation plant.
  • the gaseous, pressurized air product can in particular be nitrogen, oxygen or argon.
  • the formation in the liquid state takes place in particular in a rectification column system of the air separation plant, as explained in detail above with reference to the internal compression.
  • the air product initially formed in the liquid state can, within the scope of the present invention, in particular also be temporarily stored in one or more storage tanks.
  • the intermediate storage also takes place in particular in the liquid state.
  • At least part of the air product formed in the liquid state is used in an adjustable volume flow subjected to a pump arrangement of a pressure increase to an adjustable target pressure, after the pressure increase by heating to the target pressure in a gaseous or supercritical state (i.e. evaporated or pseudo-evaporated), and after heating or transferring to the gaseous or supercritical state as the pressurized, gaseous state Air product discharged from the air separation plant via a product line.
  • a gaseous or supercritical state i.e. evaporated or pseudo-evaporated
  • the proposed method therefore includes internal compression, as explained above, reference being made to the relevant specialist literature for further details.
  • a gaseous, pressurized air product is mentioned here, and furthermore it is mentioned that "a” or “the” air product is initially in liquid state is formed, it goes without saying that the present invention can also be used in connection with methods in which several corresponding air products are formed by internal compression.
  • other air products can be provided in liquid or gaseous state.
  • only part of an initially liquid air product can be increased in pressure by internal compression and converted into a gaseous or supercritical state, whereas another part of a corresponding air product initially formed in liquid form can be discharged from the air separation plant in a liquid state, for example, or evaporated or pseudo-evaporated without increasing the pressure can be.
  • a recognition of the operating point and a bypass control to avoid impermissible operating ranges and a final pressure limitation are provided.
  • this allows effective prevention of (permanent) cavitation of the pump.
  • the present invention includes that a setpoint for a pressure difference between a suction-side and a pressure-side pressure of the pump is specified, that an actual value of the pressure difference is determined, and that a control device is used that regulates the pressure difference by setting the pressure-side pressure.
  • a corresponding method thus does not intervene in upstream system components or their regulation, due to the advantageously only regulation of the pressure difference on the pressure side.
  • a suction-side pressure can therefore be kept constant, for which purpose a regulation is advantageously also provided within the scope of the present invention, which acts on an inlet valve, but can take place independently of the aforementioned regulation.
  • Such regulation on the suction side can also detect a pressure on the suction side of the pump.
  • a pressure on the pressure side of a corresponding inlet valve can be detected.
  • the inlet valve is set up to adjust a flow cross section upstream of the pump accordingly, in order to act in this way on the pressure on the suction side.
  • a return valve is used in the context of the present invention, which is controlled accordingly.
  • the The return valve is arranged in a return line on the pressure side of the pump.
  • the return valve and the return line are referred to as, within the scope of the present invention, the return line advantageously opens into a fluid volume from which the air product initially formed in liquid form was removed beforehand.
  • a corresponding fluid volume can be, for example, a fluid collection device or fluid removal device of a rectification column.
  • the air product, initially formed in liquid form is taken from a corresponding volume of fluid and then fed to the pump used.
  • a return flow of the corresponding pressurized fluid into the fluid volume is effected via the return line and the return valve arranged in the return line when a corresponding pressure regulation intervenes.
  • a flow cross-section in the further return line is reduced by means of the return valve when the actual value of the pressure difference is below the setpoint, and increased when the pressure difference is above the setpoint.
  • the pressure is reduced by increasing the amount of fluid returned via the return line.
  • the pressure present on the pressure side of the pump is not necessarily the product pressure. Rather, the latter can be set by using the corresponding control valve arranged further downstream in the product line, as explained above.
  • the appropriate control can in particular prevent (permanent) cavitation of the pump within the scope of the present invention, ie it can be prevented that significant amounts of gas are present in a corresponding pump, which could damage the pump.
  • a range for permissible pressure differences can be specified in each case for the speed set for setting the flow rate. This can be done, for example, by using a characteristic map and the like take place in a corresponding regulation. In such a characteristic diagram or by means of corresponding characteristic curves, a corresponding range can be defined for different mass flow values. In the context of the present invention, it is then determined whether or not the determined pressure difference lies within this specified (permissible) range. It goes without saying that the respective setpoint values for the pressure difference must lie within the permissible range.
  • a shutdown routine for shutting down the pump can be initiated.
  • This shutdown routine can include or define a delay time, for example.
  • the shutdown routine can include initiating a shutdown of the pump if, after a specified waiting time, the pressure difference is still not within the specified (permissible) range.
  • the waiting time can be, for example, one minute, two minutes, three minutes or five minutes. It is selected, for example, on the basis of a load capacity or cavitation tolerance of the pump used.
  • the waiting time can also be specified depending on the respective operating status. For example, for transient operating conditions, i.e.
  • a longer waiting time can be provided.
  • the shutdown routine and the waiting time used therein are used to ensure that unsafe operating states, in which the pump could be damaged, are reliably avoided even if the control system fails within the scope of the present invention.
  • the mass flow in which at least part of the air product initially formed in the liquid state is subjected to the pressure increase to the target pressure is set by setting a speed of a pump in a pump arrangement used in the air separation plant .
  • a speed of a pump in a pump arrangement used in the air separation plant is set by setting a speed of a pump in a pump arrangement used in the air separation plant .
  • the quantity control via the speed and an optionally provided and subsequently explained pressure control via a product valve differ from known methods, such as those in WO 2015/127648 A1 are disclosed.
  • a mass flow and a pressure of a corresponding air product are measured and a speed of an internal compression pump is controlled.
  • an amount of product can be controlled using a blow-off valve.
  • the measures used in accordance with the embodiment of the invention just explained thus differ from the known measures through the quantity control via the pump speed and the pressure control via the setting of a product valve.
  • the method offers the particular advantage that pressure fluctuations are intercepted by the rapid reaction of a control valve, while quantity changes are taken over by the slower pump control.
  • the constancy of the pressure is particularly important for the process control in the heat exchanger, so that this embodiment of the invention offers particular advantages here.
  • the method thus represents an advantageous alternative to known methods and not just an arbitrary modification.
  • the mass flow can be regulated, in particular using a mass flow control, which influences a pump speed as a manipulated variable.
  • a corresponding volume flow control can, for example, be based on a volume flow measurement as an actual variable, with this volume measurement being able to be placed before or after the control valve or also on the consumer side, downstream of the branch to the product blow-off.
  • the product pressure can be adjusted in particular by adjusting a control valve in the product line.
  • This can take place in particular using a pressure control which, based on a measured pressure value as an actual variable, carries out a corresponding adjustment of the control valve.
  • the pressure control will typically work on the basis of a measured pressure value upstream of the control valve as an actual variable, but is not limited to this.
  • the heating takes place using a main heat exchanger of the air separation plant.
  • the pump arrangement is on the cold side and the control valve is arranged on the warm side of the main heat exchanger. In this way, the product pressure can be set directly by means of the control valve, without further changes in product pressure downstream.
  • a required product pressure can therefore be precisely adhered to within the framework of the present invention within the framework of the proposed regulation.
  • variable provision of the gaseous, pressurized air product takes place within the scope of the present invention
  • a variable provision here comprising that the volume flow is set to a first volume flow value in a first operating period and the volume flow is set to a second volume flow value in a second operating period is set.
  • the second mass flow value is in particular more than twice or 5 times and up to 10 times the first mass flow value.
  • centrifugal pump or centrifugal pump can be used, as it is used in the field of cryotechnology for the treatment of cryogenic liquids.
  • such pumps can be damaged by cavitation, so that the measures proposed according to embodiments of the invention prove to be particularly advantageous here.
  • the present invention also extends to an air separation plant which is set up to carry out a method according to an embodiment explained above in the present invention.
  • an air separation plant which is set up to carry out a method according to an embodiment explained above in the present invention.
  • express reference is made to the corresponding independent patent claim and the above statements.
  • such an air separation plant has means which are set up to carry out a method in accordance with one of the configurations explained.
  • FIG. 1 shows an air separation plant, which can be operated according to an embodiment of the invention, in the form of a schematic plant diagram.
  • the air separation plant is designated 100 as a whole.
  • Air separation plants of the type shown are often described elsewhere, for example at Häring (see above) Figure 2 .3A.
  • An air separation plant for using the present invention can be designed in the most varied of ways.
  • the air separation plant 100 shown has a main air compressor 101, a pre-cooling device 102, a cleaning system 103, a post-compressor 104, a main heat exchanger 105, an expansion turbine 106, a throttle element 107 and a distillation column system, which is not designated separately.
  • the distillation column system comprises a classic double column arrangement with a high pressure column 108 and a low pressure column 109 as well as a crude argon column 110 and a pure argon column 111.
  • a feed air flow is sucked in and compressed by means of the main air compressor 101 via a filter (not designated).
  • the compressed feed air flow is that operated with cooling water Pre-cooling device 102 supplied.
  • the pre-cooled feed air stream is purified in the cleaning system 103.
  • the precooled feed air stream is freed from water and carbon dioxide.
  • the feed air flow Downstream of the cleaning system 103, the feed air flow is divided into two partial flows. One of the partial flows is completely cooled down to the pressure level of the feed air flow in the main heat exchanger 105. The other partial flow is recompressed in the booster 104 and also cooled in the main heat exchanger 105, but only to an intermediate temperature level. After it has been cooled, this so-called turbine stream is expanded to the pressure level of the completely cooled partial stream by means of the expansion turbine 106, combined with it, and fed into the high-pressure column 108.
  • an oxygen-enriched liquid bottom fraction and a nitrogen-enriched gaseous top fraction are formed as air products.
  • the oxygen-enriched liquid bottom fraction is withdrawn from the high-pressure column 108, partially used as a heating medium in a bottom evaporator of the pure argon column 110 and fed in defined proportions into a top condenser of the crude argon column 110, into a top condenser of the pure argon column 111, and directly the low pressure column 109. Fluid evaporating in the evaporation chambers of the top condensers of the crude argon column 110 and the pure argon column 111 is likewise transferred to the low-pressure column 109.
  • the gaseous nitrogen-rich top product is withdrawn from the top of the high-pressure column 108, liquefied in a main condenser 112, which creates a heat-exchanging connection between the high-pressure column 108 and the low-pressure column 109, and fed in portions as a return to the high-pressure column 108 and expanded into the low-pressure column 109.
  • An oxygen-rich liquid bottom fraction and a nitrogen-rich gaseous top fraction are formed in the low-pressure column 109.
  • the former is partially brought to liquid pressure in a pump arrangement 10 using a pump 11 in the cryogenic state, heated to this pressure in the main heat exchanger 105, converted from the liquid state into the gaseous or supercritical state, and provided as a pressurized, gaseous air product.
  • the Pressurized, gaseous air product is discharged from the air separation plant 100 by means of a product line 12 with a control valve 13.
  • a cryogenic air product in the liquid state is thus formed in the form of the liquid bottom fraction of the low-pressure column 109, which is at least partially brought to a certain pressure, here referred to as product pressure, by heating on the liquid state using the pump arrangement 10
  • Product pressure is converted into a gaseous or supercritical state (that is, vaporized or pseudo-vaporized) and is discharged from the air separation plant 100 via the product line 12 as a pressurized, gaseous air product.
  • a mass flow in which the cryogenic air product is compressed in the pump arrangement 10 and the product pressure can be as explained above and in particular with reference to FIG Figure 2 still described, can be set within the scope of the present invention.
  • a liquid nitrogen-rich stream is withdrawn from a liquid retention device at the top of the low-pressure column 109 and discharged from the air separation plant 100 as a liquid nitrogen product.
  • a gaseous nitrogen-rich stream withdrawn from the top of the low-pressure column 109 is passed through the main heat exchanger 105 and provided as a nitrogen product at the pressure of the low-pressure column 109.
  • a stream is drawn off from an upper area of the low-pressure column 109 and, after being heated in the main heat exchanger 105, used as so-called impure nitrogen in the pre-cooling device 102 or, after being heated by an electric heater, in the cleaning system 103.
  • the internal compression described above is not limited to the bottom product of the low-pressure column 109, but can alternatively or additionally take place with regard to all liquid air products formed in a corresponding air separation plant 100.
  • internally compressed nitrogen for example from the liquefied top product of the high-pressure column 108
  • internally compressed argon for example from liquid from the pure argon column 111
  • Corresponding liquids can also be stored in storage containers and removed from them.
  • Air separation plant 100 shown is limited, but can be used in all constellations in which liquid air products are formed.
  • FIG. 2 shows a control device 200 for a pump in an air separation plant according to an embodiment of the invention in a schematic representation, for example for the air separation plant 100 according to FIG Figure 1 , along with other facilities, and at the same time illustrates a corresponding regulatory procedure.
  • the regulating device 200 is set up to regulate a pump arrangement, which is designated by 10 as before.
  • a pump that is part of the pump arrangement 10 is denoted by 11 as before.
  • a plurality of pumps 11 can also be present.
  • Fluid paths or fluid lines are in Figure 2 illustrated with solid lines and arrows, controller values, manipulated variables, communication paths, measured values or measuring lines and the like with dotted lines and arrows.
  • All of the elements identified below with 201 to 214 and explained below can, as far as technically possible and advantageous, be implemented in the form of hardware or software, mechanically, electromechanically or electronically and designed as part of controllers in the form of one or more different structural units. If necessary, the elements 201 to 214 can have suitable sensors, display devices, mechanical actuators and the like. The communication between these elements can take place partially or completely using known communication structures, by means of bus systems, by means of analog or digital signals, wired and / or wireless.
  • a feed line is denoted by 14.
  • a further fluid line which is referred to here as a return line and is provided with the reference number 15
  • a further control valve which is referred to here as a return valve and is provided with the reference number 16.
  • the return line 15 leads back into the rectification column system or a corresponding tank from which the respectively treated liquid air product was withdrawn. Since in the example of the Figure 1 a withdrawal from the low-pressure column 109 takes place, its integration is here again in the form corresponding blocks are indicated with the reference number 109. The same applies to the supply line 14.
  • the position of the main heat exchanger 105 is also indicated with a corresponding reference number.
  • a non-return valve 17 is provided upstream of the control valve 12, and an inlet valve 18 is located upstream of the pump 11 in the supply line 14. It goes without saying that the arrangement also differs from the specific illustration according to FIG Figure 2 may differ.
  • a mass flow of a liquid air product conveyed using the pump 11 is set by setting a speed of the pump 11 in the pump arrangement 10. Furthermore, a pressure to which the liquid air product is brought in the pump arrangement 10 is set, in particular by setting the control valve 13 in the product line 12.
  • a pressure regulator 201 is provided with a target value that can be set manually or in some other way, for example, which controls the regulating valve 13.
  • a pressure transducer which can be part of a corresponding regulation and which, for example, detects a pressure value upstream of the regulating valve 13, is not shown.
  • the inlet valve 18 can also be adjusted via a pressure regulator 202 for adjusting an upstream pressure.
  • an anti-cavitation control is implemented in the control device 200 in order to prevent cavitation of the pump 11 due to unsuitable pressure differences at the respective speed of the pump 11. This is explained below.
  • the speed of the pump 11 is specified in the form of a speed value by means of a manual setting 203 or otherwise.
  • limits can also be set by a specification unit 204 or the specification unit 204 can exceed corresponding settings.
  • a minimum permissible speed can be specified for starting up a corresponding system and a fixed, low speed for stopping or for emptying.
  • the set speed value is made available to limit generators 206 and 207, which have a maximum permissible and a minimum for the specified speed value supply permissible differential pressure value.
  • the maximum and minimum permissible differential pressure values for different rotational speed values are specified, for example, by the manufacturer and provided in the form of characteristic curves, curves, characteristic diagrams and the like.
  • a differential pressure transmitter 205 supplies the actual differential pressure value between the suction side and the pressure side of the pump 11.
  • a shutdown routine can be initiated, as illustrated in the form of a block 208. This can include a waiting time of 120 seconds, for example. If the maximum permissible differential pressure value is still exceeded after this waiting time, the pump 11 is switched off; if this has returned to a permissible range, the shutdown routine is ended without switching off the pump 11. The same also applies in the event that the pressure falls below the minimum differential pressure value.
  • a shutdown routine can also be initiated. In certain cases, for example in transient operating states, the procedure can be different or the initiation of the shutdown routines can be prevented.
  • the values supplied by the limiters 206 and 207 are fed to a target value calculator 210.
  • the differential pressure value to be striven for, calculated by the target value calculator 210, is fed to the actual differential pressure regulator 211, which can have additional values applied to it for certain cases, for example for driving down. For example, in such cases, as illustrated in the form of an arrow from above, a different target value can be specified. In the example shown, a maximum value selector 213 is provided. This can, however, be dispensed with, in which case an output of the differential pressure regulator 211 is used directly for setting the feedback valve 16.
  • the maximum value selector 213 is also supplied with a trigger value from a pressure limiter 212, so that for the cases in which the pressure from the differential pressure controller 211 output value exceeds the trigger value of the pressure limiter 212, the return valve 16 is activated.
  • a trigger value from a pressure limiter 212
  • Such a device can be dispensed with, for example, if a maximum permissible pressure value is in any case above a theoretical maximum value of the signal from the differential pressure regulator 211.
  • the flow rate of the internally compressed air product can be adjusted by adjusting the speed of the pump 11 in the pump arrangement 10 and the product pressure can be adjusted by adjusting the control valve 13 in the product line 12, with cavitation being ensured due to the measures explained above can be prevented.

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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)
EP19020075.8A 2019-02-19 2019-02-19 Procédé et installation de séparation d'air permettant de fournir de manière variable un produit dérivé de l'air gazeux sous pression Withdrawn EP3699534A1 (fr)

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
US20070209389A1 (en) 2006-03-10 2007-09-13 Prosser Neil M Cryogenic air separation system for enhanced liquid production
US20080047298A1 (en) * 2006-04-13 2008-02-28 Horst Corduan Process and apparatus for generating a pressurized product by low-temperature air fractionation
US20090129941A1 (en) * 2007-11-16 2009-05-21 Sebastian Haas Method for controlling a pump arrangement, and pump arrangement
WO2015127648A1 (fr) 2014-02-28 2015-09-03 Praxair Technology, Inc. Distribution de courant de produit sous pression
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2980514A1 (fr) 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
US20070209389A1 (en) 2006-03-10 2007-09-13 Prosser Neil M Cryogenic air separation system for enhanced liquid production
US20080047298A1 (en) * 2006-04-13 2008-02-28 Horst Corduan Process and apparatus for generating a pressurized product by low-temperature air fractionation
US20090129941A1 (en) * 2007-11-16 2009-05-21 Sebastian Haas Method for controlling a pump arrangement, and pump arrangement
WO2015127648A1 (fr) 2014-02-28 2015-09-03 Praxair Technology, Inc. Distribution de courant de produit sous pression
US20160186930A1 (en) * 2014-02-28 2016-06-30 Praxair Technology, Inc. Pressurized product stream delivery
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2980514A1 (fr) 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Industrial Gases Processing", 2006, WILEY-VCH

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