ES2219230T3 - PROCEDURE AND DEVICE FOR OBTAINING A PRESSURE OXYGEN PRODUCT BY LOW TEMPERATURE AIR DECOMPOSITION. - Google Patents
PROCEDURE AND DEVICE FOR OBTAINING A PRESSURE OXYGEN PRODUCT BY LOW TEMPERATURE AIR DECOMPOSITION.Info
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- ES2219230T3 ES2219230T3 ES00115777T ES00115777T ES2219230T3 ES 2219230 T3 ES2219230 T3 ES 2219230T3 ES 00115777 T ES00115777 T ES 00115777T ES 00115777 T ES00115777 T ES 00115777T ES 2219230 T3 ES2219230 T3 ES 2219230T3
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- pressure
- column
- air
- oxygen
- air stream
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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
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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
- F25J3/04248—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
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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
- F25J3/04012—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
- F25J3/04018—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 main feed air
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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
- F25J3/04012—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
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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
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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- 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
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
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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
- F25J3/04248—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
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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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
- F25J3/0446—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 the heat generated by mixing two different phases
- F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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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
- 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
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
Description
Procedimiento y dispositivo para obtener un producto de oxígeno a presión por descomposición de aire a baja temperatura.Procedure and device to obtain a pressure oxygen product due to low air decomposition temperature.
La invención concierne a un procedimiento y un dispositivo para obtener un producto de oxígeno a presión por descomposición de aire a baja temperatura según los respectivos preámbulos de las reivindicaciones 1 y 9. Un procedimiento y un dispositivo de la clase citada son conocidos por el documento EP 697576 Al. En la invención se hace funcionar la columna mezcladora a una presión que es más baja que la presión de funcionamiento de la columna de alta presión del sistema de dos columnas que sirve para la separación de nitrógeno-oxígeno.The invention concerns a method and a device to obtain a pressurized oxygen product by low temperature air decomposition according to the respective preambles of claims 1 and 9. A method and a device of the aforementioned class are known from the EP document 697576 Al. In the invention the mixing column is operated at a pressure that is lower than the operating pressure of the high-pressure column of the two-column system used to the nitrogen-oxygen separation.
El sistema de rectificación de la invención puede estar construido como un sistema de dos columnas, por ejemplo como un sistema clásico de doble columna, pero también como un sistema de tres o más columnas. Además de las columnas para la separación de nitrógeno-oxígeno, dicho sistema puede presentar otros dispositivos para obtener otros componentes del aire, especialmente gases nobles (por ejemplo, criptón, xenón y/o argón).The rectification system of the invention can be built as a two column system, for example as a classic double column system, but also as a system of three or more columns. In addition to the columns for the separation of nitrogen-oxygen, said system may present other devices to obtain other air components, especially noble gases (for example, krypton, xenon and / or argon).
La fracción rica en oxígeno, que se emplea como carga para la columna mezcladora, presenta una concentración de oxígeno que es más alta que la del aire y que, por ejemplo, está en 70 a 99,5% en moles, preferiblemente 90 a 98% en moles. Por columna mezcladora se entiende una columna de contacto a contracorriente en la que una fracción gaseosa fácilmente volátil es enviada al encuentro de un líquido difícilmente volátil.The oxygen-rich fraction, which is used as load for the mixing column, has a concentration of oxygen that is higher than that of air and that, for example, is in 70 to 99.5 mol%, preferably 90 to 98 mol%. Per column mixer means a counter current contact column in which an easily volatile gaseous fraction is sent to I find a hardly volatile liquid.
El procedimiento según la invención es adecuado especialmente para la obtención de oxígeno impuro gaseoso a presión. Como oxígeno impuro se designa aquí una mezcla con un contenido de oxígeno de 99,5% en moles o menos, especialmente 70 a 99,5% en moles. Las presiones del producto son, por ejemplo, de 2,2 a 4,9 bares, preferiblemente 2,5 a 4,5 bares. Por supuesto, en caso necesario, el producto a presión puede comprimirse aún más en estado gaseoso.The process according to the invention is suitable especially for obtaining impure oxygen gas under pressure. As impure oxygen, a mixture with a content of oxygen of 99.5% in moles or less, especially 70 to 99.5% in moles Product pressures are, for example, from 2.2 to 4.9 bars, preferably 2.5 to 4.5 bars. Of course, in case necessary, the pressurized product can be compressed even more in a state gaseous.
En el documento EP 697576 A se comprime el aire total hasta aproximadamente la presión de la columna de alta presión y se expande el aire de la columna mezcladora a continuación hasta la presión de funcionamiento de dicha columna mezcladora, realizándose la expansión de una parte del aire de la columna mezcladora en una forma que produce trabajo. De este modo, la alta presión de esta corriente de aire parcial puede utilizarse ciertamente para la obtención de frío. Sin embargo, el procedimiento conocido no es energéticamente favorable en todos los casos.In EP 697576 A the air is compressed total up to about the pressure of the high pressure column and the air in the mixing column is then expanded until the operating pressure of said mixing column, performing the expansion of a part of the column air mixer in a way that produces work. In this way, the high pressure of this partial air stream can be used certainly to get cold. However, the procedure known is not energetically favorable in all cases.
Un proceso semejante se describe en el documento EP 1024464 Al no publicado todavía. Aquí se depuran unas corrientes de aire de carga primera y segunda por separado una de otra.A similar process is described in the document EP 1024464 Al not yet published. Here some currents are purified of first and second load air separately from each other.
La invención se basa en el problema de indicar un procedimiento de la clase citada al principio y un dispositivo correspondiente que presenten un consumo de energía especialmente reducido.The invention is based on the problem of indicating a class procedure cited at the beginning and a device corresponding to have an energy consumption especially reduced.
Este problema se resuelve por el hecho de que una corriente de aire total, que comprende al menos la primera y la segunda corrientes de aire de carga, es comprimida hasta una primera presión (P_{2}) que es más baja que la presión de funcionamiento (P_{HDS}) de la columna de alta presión, y es depurada bajo aproximadamente esta primera presión (p_{1}), la corriente de aire total depurada es distribuida en la primera y la segunda corrientes de aire de carga y la primera corriente de aire de carga es comprimida adicionalmente por separado de la segunda corriente de aire de carga hasta una segunda presión (p_{1}) que es al menos igual a la presión de funcionamiento (P_{HDS}) de la columna de alta presión.This problem is solved by the fact that a total air flow, comprising at least the first and the second charging air currents, is compressed until a first pressure (P2) that is lower than the operating pressure (P_ {HDS}) of the high pressure column, and is scrubbed under approximately this first pressure (p1), the current of Total purified air is distributed in the first and second charging air streams and the first charging air stream it is additionally compressed separately from the second stream of charge air to a second pressure (p1) which is at least equal to the operating pressure (P_ {HDS}) of the column of high pressure.
Por tanto, la corriente de aire total no es comprimida a la más alta presión en el sistema, sino a un valor más bajo. La parte o las partes del aire que necesitan una presión relativamente alta - especialmente el aire de la columna de alta presión - son comprimidas adicionalmente de forma deliberada por separado. De este modo, se puede tener suficiente con la aplicación de energía lo más pequeña posible durante la compresión del aire de carga.Therefore, the total air flow is not compressed at the highest pressure in the system, but at a higher value low. The part or parts of the air that need a pressure relatively high - especially high column air pressure - are additionally deliberately compressed by separated. In this way, you can have enough with the application of energy as small as possible during air compression of load.
Se logra el más pequeño gasto en aparatos cuando la primera presión es aproximadamente igual a la presión de funcionamiento de la columna mezcladora. En este caso, el aire de la columna mezcladora (segunda corriente de aire de carga) puede ser introducido en dicha columna mezcladora sin más medidas de variación de la presión.The smallest expenditure on devices is achieved when the first pressure is approximately equal to the pressure of operation of the mixing column. In this case, the air of The mixing column (second load air stream) can be introduced into said mixing column without further variation measures of pressure.
Como alternativa a esto, la primera presión puede ser más baja que la presión de funcionamiento (p_{Mis}) de la columna mezcladora. En este caso, se comprime adicionalmente la segunda corriente de aire de carga, por separado de la primera corriente de aire de carga, hasta una tercera presión (p_{3}) que es al menos igual a la presión de funcionamiento (p_{MiS}) de la columna mezcladora.As an alternative to this, the first pressure can be lower than the operating pressure (p_ {Mis}) of the mixer column In this case, the second charging air stream, separately from the first charging air flow, up to a third pressure (p 3) that is at least equal to the operating pressure (p_ {MiS}) of the mixer column
Preferiblemente, la fracción rica en oxígeno puesta a presión en estado líquido es calentada en intercambio de calor indirecto con una corriente de aire recalentada antes de cargarla en la columna mezcladora. La corriente de aire recalentada está formada, por ejemplo, por una parte del aire de carga que se encuentra a la presión de la columna de alta presión. Esta se extrae, a una temperatura intermedia, del intercambiador de calor principal en el que se enfría aire de carga hasta aproximadamente el punto de rocío, y, sin más medidas de variación de la temperatura, es puesta en intercambio de calor indirecto con el líquido rico en oxígeno. De esta manera, la temperatura del líquido que se carga en la columna mezcladora es adaptada de forma óptima a las condiciones durante el intercambio de materias a contracorriente dentro de dicha columna mezcladora.Preferably, the oxygen rich fraction Pressurized in liquid state is heated in exchange for indirect heat with a reheated air stream before Load it in the mixer column. The reheated air stream it is formed, for example, by a part of the cargo air that is found at the pressure of the high pressure column. This is extract, at an intermediate temperature, the heat exchanger main in which charge air is cooled to about dew point, and, without further temperature variation measures, it is put in indirect heat exchange with the liquid rich in oxygen. In this way, the temperature of the liquid that is charged in the mixing column is optimally adapted to the conditions during the exchange of countercurrent materials within said mixer column
En el procedimiento se genera frío de manera favorable expandiendo una tercera corriente de aire de carga en una forma productora de trabajo e introduciéndola en la columna de baja presión. De este modo, se puede aprovechar el gradiente de presión "natural" entre la primera presión u otra presión del procedimiento para compensar pérdidas de aislamiento y eventualmente licuar una parte de los productos.In the procedure cold is generated so favorable by expanding a third load air stream in a productive way of working and introducing it in the low column Pressure. In this way, the pressure gradient can be used "natural" between the first pressure or another pressure of the procedure to compensate for insulation losses and eventually Blend a portion of the products.
Preferiblemente, la tercera corriente de aire de carga es recomprimida antes de la expansión productora de trabajo, empleándose especialmente la energía mecánica generada durante la expansión productora de trabajo para el accionamiento del equipo de recompresión. Se puede utilizar aquí una combinación de turbina-booster en la que la turbina de expansión y el recompresor están acoplados mecánicamente a través de un árbol común.Preferably, the third air stream of load is recompressed before the labor-producing expansion, especially using the mechanical energy generated during the working production expansion for the operation of the equipment recompression A combination of turbine-booster in which the expansion turbine and the recompressor are mechanically coupled through a tree common.
La tercera corriente de aire de carga puede ser comprimida a la primera presión y depurada juntamente con la primera y la segunda corrientes de aire de carga. A continuación, es conducida directamente al equipo de recompresión o bien es recomprimida aún juntamente con la primera corriente de aire de carga.The third load air stream can be compressed at the first pressure and purified together with the first and the second charging air currents. The following is led directly to the recompression team or is it recompressed even together with the first air stream of load.
Como alternativa al insuflado de la tercera corriente de aire de carga en la columna de baja presión, la segunda corriente de aire de carga puede ser expandida produciendo trabajo después de su compresión adicional y antes de su alimentación a la columna mezcladora. La compresión adicional se efectúa entonces hasta una segunda presión que es netamente más alta que la presión de la columna mezcladora.As an alternative to the insufflation of the third load air current in the low pressure column, the second Charge air stream can be expanded producing work after additional compression and before feeding to the mixer column The additional compression is then performed up to a second pressure that is clearly higher than the pressure of the mixing column.
La invención concierne, además, a un dispositivo según la reivindicación 9.The invention also concerns a device according to claim 9.
Se explican seguidamente la invención y otros detalles de la misma en forma más pormenorizada haciendo referencia a ejemplos de ejecución representados en los dibujos. Muestran en éstos:The invention and others are explained below. details of it in more detailed way making reference to examples of execution represented in the drawings. Show in these:
la figura 1, un procedimiento y un dispositivo con expansión productora de trabajo de una parte del aire comprimido a la primera presión,Figure 1, a procedure and a device with working production expansion of a part of the compressed air at the first pressure,
la figura 2, un proceso modificado con expansión productora de trabajo de una parte del aire comprimido a la segunda presión,Figure 2, a modified process with expansion Working producer of one part of the compressed air to the second Pressure,
la figura 3, un procedimiento con expansión productora de trabajo del aire de la columna mezcladora yFigure 3, a procedure with expansion working producer of the mixing column air and
la figura 4, otra variante de la figura 1 sin recompresión del aire de la turbina.Figure 4, another variant of Figure 1 without turbine air recompression.
En el proceso representado en la figura 1 se lleva aire de carga 1 en un compresor de aire 2 de dos etapas con refrigeración posterior a una primera presión p_{1} de, por ejemplo, 2,7 a 3,7 bares, preferiblemente alrededor de 3,2 bares, y dicho aire de carga entra a esta presión en un equipo de depuración 3 que está formado preferiblemente por un par de adsorbedores de tamices moleculares. El aire total depurado 4 es distribuido en tres corrientes parciales 5, 6, 7.In the process represented in Figure 1, it carries load air 1 in a two-stage air compressor 2 with cooling after a first pressure p1 of, by example, 2.7 to 3.7 bars, preferably about 3.2 bars, and said loading air enters this pressure in a purification equipment 3 which is preferably formed by a pair of adsorbers of molecular sieves The total purified air 4 is distributed in three partial currents 5, 6, 7.
La primera corriente de aire de carga 5 es comprimida adicionalmente en un primer recompresor 8 a una segunda presión p_{2} de, por ejemplo, 4,4 a 7,0 bares, preferiblemente alrededor de 5,7 bares, y entra en un intercambiador de calor principal 10 después de una refrigeración posterior 9. La primera corriente de aire de carga sale del intercambiador de calor principal 10 por una tubería 11 a aproximadamente la temperatura del punto de rocío y es alimentada a una columna de alta presión 13 a través de una tubería 12. La presión de funcionamiento P_{HDS} de la columna de alta presión 13 es, por ejemplo, de 4,3 a 6,9 bares, preferiblemente alrededor de 5,6 bares. Además, el sistema de rectificación presenta una columna de baja presión 14 que se hace funcionar por debajo de, por ejemplo, 1,3 a 1,7 bares, preferiblemente alrededor de 1,5 bares.The first charge air stream 5 is additionally compressed in a first 8 to a second compressor pressure p2 of, for example, 4.4 to 7.0 bar, preferably around 5.7 bars, and enters a heat exchanger main 10 after a subsequent cooling 9. The first charging air stream exits the heat exchanger main 10 through a pipe 11 at approximately the temperature of the dew point and is fed to a high pressure column 13 to through a pipe 12. The operating pressure P_ {HDS} of the high pressure column 13 is, for example, 4.3 to 6.9 bar, preferably around 5.6 bars. In addition, the system rectification features a low pressure column 14 that is made operate below, for example, 1.3 to 1.7 bars, preferably about 1.5 bars.
La segunda corriente de aire de carga 6 es conducida también por el intercambiador de calor principal 10 a aproximadamente la primera presión p_{1} (menos pérdidas de potencia y pérdidas de presión en el equipo de depuración) y pasa finalmente a la columna mezcladora a través de una tubería 15. El punto de alimentación está inmediatamente por encima del sumidero de la columna mezcladora 16.The second charging air stream 6 is also driven by the main heat exchanger 10 a approximately the first pressure p_ {less losses of power and pressure losses in the purification equipment) and passes finally to the mixing column through a pipe 15. The power point is immediately above the sump of the mixing column 16.
La tercera corriente parcial 7 es recomprimida desde aproximadamente la primera presión p_{1} en un segundo recompresor 17 hasta una tercera presión p_{3} de, por ejemplo, 3,8 a 5,6 bares, preferiblemente alrededor de 4,7 bares, y, después de una refrigeración posterior 18, es conducida por la tubería 19 al extremo caliente del intercambiador de calor principal. Sin embargo, es enfriada únicamente hasta una temperatura intermedia y ya antes del extremo frío es retirada nuevamente del intercambiador de calor principal 10 por una tubería 50 y expandida produciendo trabajo en una turbina 20. El aire expandido 21 es insuflado en la columna de baja presión 14. El recompresor 17 y la turbina 20 están acoplados mecánicamente de forma directa.The third partial stream 7 is recompressed from about the first pressure p1 in a second recompressor 17 to a third pressure p3 of, for example, 3.8 to 5.6 bars, preferably about 4.7 bars, and then of a subsequent cooling 18, is conducted by the pipe 19 to hot end of the main heat exchanger. Nevertheless, it is cooled only to an intermediate temperature and before from the cold end it is removed again from the heat exchanger main 10 by a 50 pipe and expanded producing work in a turbine 20. The expanded air 21 is blown into the column of low pressure 14. The compressor 17 and the turbine 20 are coupled mechanically directly.
El sistema de rectificación está construido en los ejemplos de ejecución como un aparato Linde clásico de doble columna con un condensador-evaporador 22 en calidad de condensador principal. Sin embargo, la invención puede utilizarse también en sistemas de rectificación con otra configuración de condensador y/o de columna.The rectification system is built in Execution examples as a classic double Linde device column with a condenser-evaporator 22 in quality of main condenser. However, the invention can be used. also in rectification systems with other configuration of condenser and / or column.
Líquido 23 enriquecido en oxígeno procedente del sumidero de la columna de alta presión 13 es enfriado en un primer aparato de subenfriamiento a contracorriente 24 y alimentado, después de una estrangulación 25, a la columna de baja presión 14 en un punto intermedio 26. Nitrógeno gaseoso 27 procedente de la cabeza de la columna de alta presión 13 puede ser calentado en una parte 28 en el intercambiador de calor principal 10 y recuperado como producto de nitrógeno a presión 29. El resto 30 es condensado de forma sustancialmente completa en el condensador principal 22. El nitrógeno líquido 31 obtenido de este modo es entregado al menos en una parte 32 como retorno a la columna de alta presión 13. En caso necesario, se puede retirar otra parte 33 como producto líquido. Un líquido intermedio 34 (nitrógeno impuro) de la columna de alta presión sirve, después del subenfriamiento 24 y la estrangulación 35, como retorno para la columna de baja presión. Nitrógeno impuro gaseoso 36 procedente de la cabeza de la columna de baja presión es calentado en los intercambiadores de calor 24 y 10 y retirado finalmente por la tubería 37. Como se ha representado, este nitrógeno puede ser utilizado como gas de regeneración para el equipo de depuración 3.Liquid 23 enriched in oxygen from the high pressure column drain 13 is cooled in a first counter-current subcooling apparatus 24 and powered, after a throttle 25, to the low pressure column 14 in an intermediate point 26. Nitrogen gas 27 from the head of the high pressure column 13 can be heated in one part 28 in the main heat exchanger 10 and recovered as nitrogen product under pressure 29. The remainder 30 is condensed from substantially complete form in the main capacitor 22. The liquid nitrogen 31 obtained in this way is delivered at least in a part 32 as a return to the high pressure column 13. In case If necessary, another part 33 can be removed as a liquid product. A intermediate liquid 34 (impure nitrogen) of the high column pressure serves, after subcooling 24 and strangulation 35, as a return for the low pressure column. Impure nitrogen gas 36 coming from the head of the low pressure column is heated in heat exchangers 24 and 10 and removed finally by pipe 37. As represented, this nitrogen can be used as a regeneration gas for the debugging equipment 3.
Nitrógeno líquido 38 es retirado del sumidero de la columna de baja presión, puesto a una presión de, por ejemplo, 5,7 a 6,5 bares, preferiblemente alrededor de 6,1 bares, en una bomba 39, calentado en un segundo aparato de subenfriamiento a contracorriente 40 y, finalmente, entregado (41) a la cabeza de la columna mezcladora 16. En el segundo aparato de subenfriamiento a contracorriente 40 se enfría especialmente una corriente de aire recalentada 42 que se deriva de la primera corriente de aire de carga aguas arriba del extremo frío del intercambiador de calor principal, concretamente a una temperatura intermedia que es más baja que la temperatura de entrada de la turbina 20. Después de su enfriamiento a través de una tubería 43, esta corriente de aire se reúne nuevamente con la primera corriente de aire de carga 11. A través de la válvula 44 se ajusta la cantidad de la corriente de aire que circula por el segundo aparato de subenfriamiento a contracorriente.Liquid nitrogen 38 is removed from the sump of the low pressure column, set at a pressure of, for example, 5.7 to 6.5 bars, preferably around 6.1 bars, in one pump 39, heated in a second subcooling apparatus a countercurrent 40 and finally delivered (41) to the head of the mixer column 16. In the second subcooling apparatus a countercurrent 40 especially cools an air stream reheated 42 that is derived from the first air stream of load upstream of the cold end of the heat exchanger principal, specifically at an intermediate temperature that is more lower than the turbine inlet temperature 20. After its cooling through a pipe 43, this air stream is meets again with the first load air stream 11. A through the valve 44 the amount of the current of air flowing through the second subcooling apparatus a countercurrent
Oxígeno gaseoso impuro a presión 51 es retirado de la cabeza de la columna mezcladora 16, calentado en el intercambiador de calor principal 10 y recuperado como producto 52. Se extraen de la columna mezcladora un líquido de sumidero 45 y un líquido intermedio 46 y se alimentan éstos a un punto adecuado de la columna de baja presión 14 a través de las tuberías 47 y 48, respectivamente.Impure gaseous oxygen under pressure 51 is removed of the head of the mixing column 16, heated in the main heat exchanger 10 and recovered as product 52. A sump liquid 45 and a liquid are removed from the mixer column. intermediate liquid 46 and these are fed to a suitable point of the low pressure column 14 through pipes 47 and 48, respectively.
La figura 2 se diferencia de la figura 1 únicamente porque la tercera corriente de aire de carga 207 es comprimida adicionalmente junto con la segunda corriente de aire de carga en el primer recompresor 108. De este modo, se alcanza una presión de entrada más alta en la turbina 20 y, por consiguiente, se genera más frío.Figure 2 differs from figure 1 solely because the third load air stream 207 is additionally compressed together with the second air stream of load on the first recompressor 108. In this way, a higher inlet pressure in the turbine 20 and therefore It generates colder.
En la variante de la figura 3 se hace funcionar el equipo de depuración a una primera presión p_{1}' que es más alta que la presión de funcionamiento p_{MiS} de la columna mezcladora. La primera presión p_{1}' es aquí de, por ejemplo, 2,7 a 3,7 bares, preferiblemente alrededor de 3,2 bares. La segunda corriente de aire de carga 306 se expande aquí aguas arriba de su alimentación a la columna mezcladora. No existe una tercera corriente de aire de carga que se insufle en la columna de baja presión. La segunda corriente de aire de carga 306 es comprimida adicionalmente, aguas abajo de su derivación del aire total depurado, en el segundo recompresor 317, el cual es accionado por la turbina 320. La segunda corriente de aire de carga 349 comprimida adicionalmente a, por ejemplo, 3,8 a 5,6 bares, preferiblemente alrededor de 4,7 bares, es alimentada a la turbina 320 por una tubería 350 y expandida allí produciendo trabajo hasta aproximadamente la presión p_{MiS} de la columna mezcladora.In the variant of figure 3 it is operated the purification equipment at a first pressure p_ {1} 'which is more high than the operating pressure p_ {MiS} of the column mixer. The first pressure p_ {1} 'is here of, for example, 2.7 at 3.7 bars, preferably around 3.2 bars. The second charge air stream 306 expands here upstream of its mixer column feed. There is no third load air flow that is blown into the low column Pressure. The second charge air stream 306 is compressed additionally, downstream of its total air bypass purified, in the second 317 recompressor, which is powered by the turbine 320. The second charge air stream 349 compressed in addition to, for example, 3.8 to 5.6 bars, preferably around 4.7 bars, it is fed to turbine 320 by a 350 pipe and expanded there producing work up approximately the pressure p_ {MiS} of the mixing column.
Análogamente a lo que ocurre en la figura 3, en el procedimiento de la figura 4 al equipo de depuración 3 se hace funcionar a una primera presión especialmente baja p_{11}'' de, por ejemplo, 2,7 a 3,7 bares, preferiblemente alrededor de 3,2 bares. Al igual que en la figura 1, la turbina 420 es solicitada con una tercera corriente de aire de carga 407, 450 que, no obstante, no se recomprime aquí, sino que se expande directamente produciendo trabajo desde aproximadamente la primera presión p_{1}'' hasta aproximadamente la presión de la columna de baja presión. El recompresor 418 accionado por la turbina es utilizado aquí para comprimir adicionalmente la segunda corriente de aire de carga hasta la segunda presión pe, la cual es aproximadamente igual a la presión de funcionamiento p_{MiS} de la columna mezcladora.Similarly to what happens in Figure 3, in the procedure of figure 4 to the debugging equipment 3 is done operate at a particularly low first pressure p_ {11} '' of, for example, 2.7 to 3.7 bar, preferably around 3.2 pubs. As in Figure 1, turbine 420 is requested with a third load air stream 407, 450 which, however, it is not recompressed here, but it expands directly producing work from approximately the first pressure p_ {1} '' to approximately the pressure of the low pressure column. The 418 turbine powered compressor is used here to additionally compress the second charge air stream until the second pressure pe, which is approximately equal to the pressure operating p_ {MiS} of the mixer column.
En todos los ejemplos de ejecución el compresor de aire y el recompresor 8, 108 se han construido de preferencia conjuntamente como una máquina de tres etapas. Expresado de otra manera, la compresión adicional de la primera corriente de aire de carga se realiza en la tercera etapa de una máquina, cuyas etapas primera y segunda sirven para la compresión del aire aguas arriba del equipo de depuración 3. Como alternativa a esto, esta máquina puede estar construida también con cuatro etapas, estando dispuestas en este caso las tres primeras etapas delante del equipo de depuración 3.In all the execution examples the compressor air and the recompressor 8, 108 have been built preferably together as a three stage machine. Expressed from another way, the additional compression of the first air stream of loading is done in the third stage of a machine, whose stages first and second serve for upstream air compression of debugging equipment 3. As an alternative to this, this machine it can also be built with four stages, being arranged in this case the first three stages in front of the team debugging 3.
Claims (9)
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DE10015602A DE10015602A1 (en) | 2000-03-29 | 2000-03-29 | Method and device for obtaining a printed product by low-temperature separation of air |
DE10015602 | 2000-03-29 |
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ES00115777T Expired - Lifetime ES2219230T3 (en) | 2000-03-29 | 2000-07-21 | PROCEDURE AND DEVICE FOR OBTAINING A PRESSURE OXYGEN PRODUCT BY LOW TEMPERATURE AIR DECOMPOSITION. |
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US (1) | US20010052244A1 (en) |
EP (1) | EP1139046B1 (en) |
KR (1) | KR20010093765A (en) |
CN (1) | CN1179181C (en) |
AT (1) | ATE265032T1 (en) |
DE (2) | DE10015602A1 (en) |
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DE102007031765A1 (en) | 2007-07-07 | 2009-01-08 | Linde Ag | Process for the cryogenic separation of air |
DE102007031759A1 (en) | 2007-07-07 | 2009-01-08 | Linde Ag | Method and apparatus for producing gaseous pressure product by cryogenic separation of air |
DE102009034979A1 (en) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Method for producing pressurized oxygen by evaporating liquid oxygen using a copper and nickel heat exchanger block |
EP2312248A1 (en) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Method and device for obtaining pressurised oxygen and krypton/xenon |
EP2553370B1 (en) | 2010-03-26 | 2019-05-15 | Linde Aktiengesellschaft | Device for the cryogenic separation of air |
DE102010012920A1 (en) | 2010-03-26 | 2011-09-29 | Linde Aktiengesellschaft | Apparatus for the cryogenic separation of air |
DE102011114090A1 (en) * | 2010-11-09 | 2012-05-10 | Linde Aktiengesellschaft | Method for cryogenic separation of air in distillation column-system for nitrogen-oxygen separation, involves withdrawing liquid from high-pressure column in flowing manner and discharging liquid into low-pressure column |
DE102010052544A1 (en) | 2010-11-25 | 2012-05-31 | Linde Ag | Process for obtaining a gaseous product by cryogenic separation of air |
DE102010052545A1 (en) | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Method and apparatus for recovering a gaseous product by cryogenic separation of air |
DE102011015233A1 (en) | 2011-03-25 | 2012-09-27 | Linde Ag | Apparatus for the cryogenic separation of air |
DE102011015430A1 (en) | 2011-03-29 | 2012-10-04 | Linde Aktiengesellschaft | Method and apparatus for producing flat gas |
DE102011015429A1 (en) | 2011-03-29 | 2012-10-04 | Linde Ag | Method involves for operating rebox burner, involves removing gaseous oxygen stream from upper region of mixing column and leading out oxygen product used for production of gas mixture |
EP2520886A1 (en) | 2011-05-05 | 2012-11-07 | Linde AG | Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air |
DE102011112909A1 (en) | 2011-09-08 | 2013-03-14 | Linde Aktiengesellschaft | Process and apparatus for recovering steel |
EP2600090B1 (en) | 2011-12-01 | 2014-07-16 | Linde Aktiengesellschaft | Method and device for generating pressurised oxygen by cryogenic decomposition of air |
DE102011121314A1 (en) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator |
DE102012017484A1 (en) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Process and plant for the production of liquid and gaseous oxygen products by cryogenic separation of air |
DE102012017488A1 (en) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements |
BR112015009379A2 (en) * | 2012-11-02 | 2017-07-04 | Linde Ag | process for low temperature air separation in an air separation plant and air separation plant |
DE102012021694A1 (en) | 2012-11-02 | 2014-05-08 | Linde Aktiengesellschaft | Process for the cryogenic separation of air in an air separation plant and air separation plant |
DE102013002094A1 (en) | 2013-02-05 | 2014-08-07 | Linde Aktiengesellschaft | Method for producing liquid and gaseous oxygen by low temperature separation of air in air separation system in industrial application, involves feeding feed air flow to portion in mixed column and to another portion in separating column |
WO2014154339A2 (en) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
EP2784420A1 (en) | 2013-03-26 | 2014-10-01 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
EP2801777A1 (en) | 2013-05-08 | 2014-11-12 | Linde Aktiengesellschaft | Air separation plant with main compressor drive |
DE102013017590A1 (en) | 2013-10-22 | 2014-01-02 | Linde Aktiengesellschaft | Method for recovering methane-poor fluids in liquid air separation system to manufacture air product, involves vaporizing oxygen, krypton and xenon containing sump liquid in low pressure column by using multi-storey bath vaporizer |
EP2963367A1 (en) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Method and device for cryogenic air separation with variable power consumption |
TR201808162T4 (en) | 2014-07-05 | 2018-07-23 | Linde Ag | Method and apparatus for recovering a pressurized gas product by decomposing air at low temperature. |
EP2963369B1 (en) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
PL2963370T3 (en) | 2014-07-05 | 2018-11-30 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
DE102015015684A1 (en) | 2015-12-03 | 2016-07-21 | Linde Aktiengesellschaft | Process for the cryogenic separation of air and air separation plant |
EP3179186A1 (en) | 2015-12-07 | 2017-06-14 | Linde Aktiengesellschaft | Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus |
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CN114413571A (en) * | 2022-01-24 | 2022-04-29 | 四川空分集团工程有限公司 | Low energy consumption low pressure oxygen air separation plant |
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US5454227A (en) * | 1994-08-17 | 1995-10-03 | The Boc Group, Inc. | Air separation method and apparatus |
US5551258A (en) * | 1994-12-15 | 1996-09-03 | The Boc Group Plc | Air separation |
DE19815885A1 (en) * | 1998-04-08 | 1999-10-14 | Linde Ag | Air separation method producing gas, or gas and liquid e.g. for steel plant |
-
2000
- 2000-03-29 DE DE10015602A patent/DE10015602A1/en not_active Withdrawn
- 2000-07-21 ES ES00115777T patent/ES2219230T3/en not_active Expired - Lifetime
- 2000-07-21 EP EP00115777A patent/EP1139046B1/en not_active Expired - Lifetime
- 2000-07-21 AT AT00115777T patent/ATE265032T1/en not_active IP Right Cessation
- 2000-07-21 DE DE50006148T patent/DE50006148D1/en not_active Expired - Fee Related
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- 2001-03-28 CN CNB01109513XA patent/CN1179181C/en not_active Expired - Fee Related
- 2001-03-29 KR KR1020010016494A patent/KR20010093765A/en active IP Right Grant
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EP1139046A1 (en) | 2001-10-04 |
CN1320798A (en) | 2001-11-07 |
CN1179181C (en) | 2004-12-08 |
DE10015602A1 (en) | 2001-10-04 |
DE50006148D1 (en) | 2004-05-27 |
ATE265032T1 (en) | 2004-05-15 |
KR20010093765A (en) | 2001-10-29 |
US20010052244A1 (en) | 2001-12-20 |
EP1139046B1 (en) | 2004-04-21 |
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