ES2675668T3 - Production process of a pressurized air gas by cryogenic distillation - Google Patents
Production process of a pressurized air gas by cryogenic distillation Download PDFInfo
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- ES2675668T3 ES2675668T3 ES12717421.7T ES12717421T ES2675668T3 ES 2675668 T3 ES2675668 T3 ES 2675668T3 ES 12717421 T ES12717421 T ES 12717421T ES 2675668 T3 ES2675668 T3 ES 2675668T3
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- air
- overpressure
- exchange line
- compressor
- intermediate temperature
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
- F25J3/04096—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of argon or argon enriched stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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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
- F25J3/04296—Claude expansion, i.e. expanded into the main or 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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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
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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- 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
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/54—Oxygen production with multiple pressure O2
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/04—Multiple expansion turbines in parallel
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Proceso de separación de aire por destilación criogénica en una instalación que comprende un sistema de columnas (31, 33), de las cuales una columna (31) opera a la presión más elevada denominada la media presión, en el cual: - todo el aire es llevado a una alta presión, superior en al menos 3 bares a la media presión, depurado a esta presión en una unidad de depuración (7) - todo el aire es enviado a la temperatura de salida de la unidad de depuración a una línea de intercambio (11); - todo el aire depurado es enfriado en la línea de intercambio (11) y una parte del aire depurado es sobrepresionada por medio de al menos un primer compresor de sobrepresión (15) de una sola etapa y que aspira a una primera temperatura intermedia de la línea de intercambio; - al menos una parte del aire sobrepresionado en el primer compresor de sobrepresión es sobrepresionada por medio de al menos un segundo compresor de sobrepresión (25) de una sola etapa y que aspira a una segunda temperatura intermedia de la línea de intercambio y es reenviado a la línea de intercambio donde se enfría, después se licua, eventualmente en el extremo frío de la línea de intercambio, y es enviado al sistema de columnas después de su expansión; - otra parte del aire depurado bajo la presión alta es enfriado en la línea de intercambio, después, al menos en parte, expandida en al menos dos turbinas (17, 27) que tienen una o dos temperaturas de entrada que es una temperatura intermedia o que son dos temperaturas intermedias de la línea de intercambio, y después enviada al sistema de columnas para ser separada; - el trabajo liberado por la expansión del aire se utiliza, al menos parcialmente, para la compresión criogénica efectuada por el primer y el segundo compresor de sobrepresión acoplando el primer compresor de sobrepresión a una de las dos turbinas y el segundo compresor de sobrepresión a la otra de las dos turbinas; - oxígeno líquido es presurizado a una presión inferior o igual a 16 bares preferentemente entre 10 y 16 bares, y se vaporiza en la línea de intercambio caracterizado por que la parte del aire sobrepresionada en el primer compresor de sobrepresión constituye entre 10% y 35% del aire depurado y la parte del aire expandida en al menos dos turbinas constituye entre 65% y 90% del aire depurado, la parte del aire sobrepresionada en el primer compresor de sobrepresión es enfriada en la línea de intercambio aguas arriba del segundo compresor de sobrepresión, un dispositivo de disipación de energía (22, 24) está acoplado a al menos uno de los compresores de sobrepresión, la primera temperatura intermedia difiere de la segunda temperatura intermedia en como máximo 10 ºC y las primera y segunda temperaturas intermedias están comprendidas entre -145 ºC y -165 ºC y las temperaturas de salida del primer y del segundo compresor de sobrepresión (15, 25) están entre -110 ºC y -150 ºC.Process of separation of air by cryogenic distillation in an installation comprising a system of columns (31, 33), of which a column (31) operates at the highest pressure called the medium pressure, in which: - all the air it is brought to a high pressure, higher by at least 3 bars at medium pressure, purified at this pressure in a purification unit (7) - all air is sent at the outlet temperature of the purification unit to a line of exchange (11); - all the purified air is cooled in the exchange line (11) and a part of the purified air is overpressured by means of at least a first single-stage overpressure compressor (15) that aspires to a first intermediate temperature of the exchange line; - at least a part of the overpressure air in the first overpressure compressor is overpressured by means of at least a second single stage overpressure compressor (25) and which aspires to a second intermediate temperature of the exchange line and is forwarded to the exchange line where it cools, then liquefies, eventually at the cold end of the exchange line, and is sent to the column system after its expansion; - another part of the purified air under high pressure is cooled in the exchange line, then, at least in part, expanded in at least two turbines (17, 27) having one or two inlet temperatures that is an intermediate temperature or which are two intermediate temperatures of the exchange line, and then sent to the column system to be separated; - the work released by the air expansion is used, at least partially, for the cryogenic compression carried out by the first and the second overpressure compressor by coupling the first overpressure compressor to one of the two turbines and the second overpressure compressor to the another of the two turbines; - liquid oxygen is pressurized at a pressure of less than or equal to 16 bar, preferably between 10 and 16 bar, and is vaporized in the exchange line characterized in that the part of the overpressured air in the first overpressure compressor constitutes between 10% and 35% of the purified air and the part of the expanded air in at least two turbines constitutes between 65% and 90% of the purified air, the part of the overpressured air in the first overpressure compressor is cooled in the exchange line upstream of the second overpressure compressor , an energy dissipation device (22, 24) is coupled to at least one of the overpressure compressors, the first intermediate temperature differs from the second intermediate temperature by a maximum of 10 ° C and the first and second intermediate temperatures are comprised between - 145 ° C and -165 ° C and the outlet temperatures of the first and second overpressure compressors (15, 25) are between -110 ° C and -150 ºC.
Description
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DESCRIPCIONDESCRIPTION
Proceso de producción de un gas de aire a presión por destilación criogénicaProduction process of a pressurized air gas by cryogenic distillation
La presente invención se relaciona con un proceso de producción de un gas de aire a presión por destilación criogénica.The present invention relates to a process of producing a pressurized air gas by cryogenic distillation.
Un objetivo de la invención es proponer una alternativa para realizar esquemas de proceso que permitan mejorar los costes de instalación de los aparatos de separación de aire para una producción de oxígeno entre 10 y 16 bares, preferentemente entre 14 y 16 bares, así pues, del orden de 15 bares.An objective of the invention is to propose an alternative to carry out process schemes that allow to improve the installation costs of the air separation apparatus for an oxygen production between 10 and 16 bars, preferably between 14 and 16 bars, thus, of the Order of 15 bars.
El estado de la técnica industrial, para los aparatos que producen oxígeno bajo presión del orden de 15 bares está constituido por aparatos “a bomba”, que utilizan un compresor de aire principal a una presión del orden de 6 bares aproximadamente, y un compresor de sobrepresión de aire que comprime una parte del caudal de aire a una presión del orden de 35-40 bares. Pero esta solución no está disponible para aparatos de tamaños pequeños, para los cuales la combinación de caudal pequeño a sobrepresionar y de una presión de descarga muy elevada lleva a una caudal real a la salida del compresor de sobrepresión demasiado pequeño para ser realizable tecnológicamente.The state of the art, for devices that produce oxygen under a pressure of the order of 15 bars is constituted by "pump" devices, which use a main air compressor at a pressure of about 6 bars, and a compressor of air overpressure that compresses a part of the air flow at a pressure of the order of 35-40 bar. But this solution is not available for devices of small sizes, for which the combination of small flow to overpressure and a very high discharge pressure leads to a real flow at the outlet of the overpressure compressor too small to be technologically feasible.
Por consiguiente, para los aparatos pequeños, se debe recurrir a la utilización de compresores de oxígeno, costosos.Therefore, for small appliances, expensive oxygen compressors must be used.
La solución propuesta permite reducir los costes para tales aparatos, por la utilización de un compresor de aire único, a una presión de descarga moderadamente elevada, lo que propone una ventaja competitiva con respecto a las dos soluciones precedentes: unicidad del compresor y evitación de un compresor de oxígeno costoso.The proposed solution allows to reduce the costs for such devices, by using a single air compressor, at a moderately high discharge pressure, which proposes a competitive advantage over the two previous solutions: compressor uniqueness and avoidance of a expensive oxygen compressor.
El documento de patente de EE.UU. US-A-20050126221 describe un proceso de separación de aire. Para producir oxígeno bajo presión, dos compresores de sobrepresión en serie que comprimen el aire a temperaturas intermedias del intercambiador principal, la temperatura de entrada del primer compresor de sobrepresión siendo más caliente que la temperatura de salida del segundo compresor de sobrepresión. Un grupo frigorífico se utiliza para rebajar la temperatura de entrada del segundo compresor de sobrepresión, aumentando así la complejidad del proceso.U.S. Patent Document US-A-20050126221 describes an air separation process. To produce oxygen under pressure, two series overpressure compressors that compress the air at intermediate temperatures of the main exchanger, the inlet temperature of the first overpressure compressor being warmer than the outlet temperature of the second overpressure compressor. A refrigeration unit is used to lower the inlet temperature of the second overpressure compressor, thereby increasing the complexity of the process.
El documento de patente de EE.UU. US-A-20060010912 describe un proceso de separación de aire en el cual aire a media presión es sobrepresionado en dos compresores de sobrepresión fríos en serie.U.S. Patent Document US-A-20060010912 describes an air separation process in which medium pressure air is overpressured in two series cold overpressure compressors.
Los dos compresores de sobrepresión no deben estar acoplados a una turbina, ya que las turbinas del proceso no funcionan más que durante una marche particular que permite fabricar el líquido. En funcionamiento nominal, el proceso es mantenido en frío par añadido de líquido criogénico.The two overpressure compressors must not be coupled to a turbine, since the process turbines only work during a particular run that allows the liquid to be manufactured. In nominal operation, the process is kept cold added torque of cryogenic liquid.
Todas las presiones son presiones absolutas.All pressures are absolute pressures.
Según la invención, todo el aire es llevado a alta presión (sensiblemente más alta que la presión de la columna de media presión, es decir, superior en al menos 3 bares a la media presión) y depurado a esta presión, y después dividido en al menos partes. Sólo una fracción del aire, la fracción que se licua posteriormente au extremo frío de la línea de intercambio principal, sufre una sucesión de compresiones criogénicas de forma que se lleve este caudal a una presión suficiente para permitir la vaporización de oxígeno a la presión deseada. Preferentemente, el resto del aire es expandido en al menos una turbina a la presión de la columna de media presión. Al menos una parte del trabajo liberado por la expansión del aire se utiliza para la compresión criogénica.According to the invention, all the air is carried at high pressure (significantly higher than the pressure of the medium pressure column, that is, at least 3 bars above the medium pressure) and purified at this pressure, and then divided into At least parts. Only a fraction of the air, the fraction that is subsequently liquefied at the cold end of the main exchange line, undergoes a succession of cryogenic compressions so that this flow is brought to a sufficient pressure to allow the vaporization of oxygen at the desired pressure. Preferably, the rest of the air is expanded in at least one turbine at the pressure of the medium pressure column. At least part of the work released by air expansion is used for cryogenic compression.
El documento de patente de EE.UU. US-A-5475980 describe un proceso según el preámbulo de la reivindicación 1. Según un objeto de la invención, se prevé un proceso según la reivindicación 1.U.S. Patent Document US-A-5475980 describes a process according to the preamble of claim 1. According to an object of the invention, a process according to claim 1 is provided.
Según otras características opcionales:According to other optional features:
- las dos turbinas tienen temperaturas de entrada iguales o diferentes, constituidas por la tercera temperatura intermedia y una cuarta temperatura intermedia de la línea de intercambio;- the two turbines have the same or different inlet temperatures, consisting of the third intermediate temperature and a fourth intermediate temperature of the exchange line;
- la tercera temperatura es inferior a la primera temperatura;- the third temperature is lower than the first temperature;
- la tercera temperatura difiere de la cuarta temperatura en como máximo 20 °C, incluso en como máximo 10 °C;- the third temperature differs from the fourth temperature by a maximum of 20 ° C, even at a maximum of 10 ° C;
- la primera temperatura es superior a la segunda temperatura;- the first temperature is higher than the second temperature;
- la primera temperatura es inferior o igual a la segunda temperatura;- the first temperature is less than or equal to the second temperature;
- se disipa una parte de la energía generada por al menos una de las turbinas;- a part of the energy generated by at least one of the turbines is dissipated;
- se disipa una parte de la energía por medio de un sistema de freno hidráulico conectado a la turbina;- a part of the energy is dissipated by means of a hydraulic brake system connected to the turbine;
- una parte del aire se licua a la alta presión, preferentemente en la línea de intercambio;- a part of the air is liquefied at high pressure, preferably in the exchange line;
22
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45Four. Five
50fifty
- el aire de al menos una de las turbinas es enviado a la columna que opera a la presión más elevada;- the air of at least one of the turbines is sent to the column operating at the highest pressure;
- todo el aire sobrepresionado en el primer compresor de sobrepresión es enviado al segundo compresor de sobrepresión;- all the overpressure air in the first overpressure compressor is sent to the second overpressure compressor;
- todo el aire depurado en la unidad de depuración es enviado a la línea de intercambio a la presión de salida de la unidad de depuración;- all the purified air in the purification unit is sent to the exchange line at the outlet pressure of the purification unit;
- el sistema comprende una doble columna de separación de aire que comprende una primera columna y una segunda columna que opera a presión más baja que la primera, siendo enviado el aire expandido en las dos turbinas a la primera columna;- the system comprises a double air separation column comprising a first column and a second column operating at a lower pressure than the first, the expanded air being sent in the two turbines to the first column;
- la primera temperatura es más fría que la temperatura de salida del segundo compresor de sobrepresión;- the first temperature is cooler than the output temperature of the second overpressure compressor;
- las temperaturas de salida del primer y del segundo compresor de sobrepresión están entre -125 °C y -145 °C.- the outlet temperatures of the first and second overpressure compressors are between -125 ° C and -145 ° C.
La invención se describirá con más detalle refiriéndose a la figura que ilustra un proceso de separación de aire según la invención.The invention will be described in more detail by referring to the figure illustrating an air separation process according to the invention.
Un caudal de aire 1 es comprimido en un compresor principal 3 hasta una presión al menos 3 bares por encima de la presión de la columna 31, que es la columna de media presión de una doble columna de separación de aire por destilación criogénica. El aire comprimido es depurado en una unidad de depuración 7 para formar el caudal depurado 9. El caudal depurado es enviado a la línea de intercambio 11 sin haber sido enfriado y en la línea de intercambio se enfría hasta una primera temperatura intermedia. A esta temperatura, el aire es dividido en una parte 13 y una parte 14. La parte 13 se mete en un solo primer compresor 15 que tiene una única etapa a la primera temperatura intermedia donde aquella es sobrepresionada. El aire sobrepresionado es enviado a la línea de intercambio 11 donde se enfría de nuevo hasta una segunda temperatura intermedia, inferior a la primera temperatura intermedia. A esta segunda temperatura intermedia, al menos una parte del aire sobrepresionado en el compresor de sobrepresión 15, incluso todo el aire 13, es sobrepresionada en un solo segundo compresor 25 que tiene una única etapa.An air flow rate 1 is compressed in a main compressor 3 to a pressure at least 3 bar above the pressure of column 31, which is the medium pressure column of a double column of air separation by cryogenic distillation. The compressed air is purified in a purification unit 7 to form the purified flow 9. The purified flow is sent to the exchange line 11 without being cooled and in the exchange line it is cooled to a first intermediate temperature. At this temperature, the air is divided into a part 13 and a part 14. Part 13 gets into a single first compressor 15 which has a single stage at the first intermediate temperature where it is overpressured. The overpressured air is sent to the exchange line 11 where it is cooled again to a second intermediate temperature, lower than the first intermediate temperature. At this second intermediate temperature, at least a part of the overpressured air in the overpressure compressor 15, including all the air 13, is overpressured in a single second compressor 25 having a single stage.
La primera temperatura intermedia difiere de la segunda temperatura en como máximo 10 °C y las primera y seguida temperaturas están comprendidas entre -145 °C y -165 °C.The first intermediate temperature differs from the second temperature by a maximum of 10 ° C and the first and subsequent temperatures are between -145 ° C and -165 ° C.
La primera temperatura intermedia puede, eventualmente, ser superior o igual a la segunda temperatura intermedia.The first intermediate temperature may, eventually, be greater than or equal to the second intermediate temperature.
Cada una de las temperaturas de salida de los compresores de sobrepresión 15, 25 está entre -110 °C y -150 °C, preferentemente entre -125 °C y -145 °C.Each of the outlet temperatures of the overpressure compressors 15, 25 is between -110 ° C and -150 ° C, preferably between -125 ° C and -145 ° C.
El caudal doblemente sobrepresionado 13 es reenviado a la línea de intercambio a la presión requerida para la vaporización de un caudal de oxígeno bajo presión. El caudal sobrepresionado 13 se enfría a esta presión hasta el extremo frío de la línea de intercambio 11 y se condensa. A la salida del intercambiador, el caudal es expandido y es enviado a la columna de media presión 31.The double overpressure flow 13 is forwarded to the exchange line at the pressure required for the vaporization of an oxygen flow under pressure. The overpressure flow rate 13 is cooled at this pressure to the cold end of the exchange line 11 and condenses. At the outlet of the exchanger, the flow rate is expanded and sent to the medium pressure column 31.
El resto del aire 14 es dividido en dos o tres partes. Según una variante, todo el aire 14 es dividido en dos partes. Una parte 19 es enviada a una turbina 17 que tiene una temperatura de entrada que es una tercera temperatura intermedia de la línea de intercambio, y después es enviada en forma gaseosa a la columna de media presión 31. Otra parte 21 es enviada a una turbina 27 que tiene una temperatura de entrada que es una cuarta temperatura intermedia de la línea de intercambio, superior a la tercera temperatura, y después es enviada en forma gaseosa a la columna de media presión 31. Preferentemente, las partes 19, 21 son mezcladas para formar un solo caudal 23.The rest of the air 14 is divided into two or three parts. According to a variant, all air 14 is divided into two parts. A part 19 is sent to a turbine 17 which has an inlet temperature that is a third intermediate temperature of the exchange line, and then is gaseous sent to the medium pressure column 31. Another part 21 is sent to a turbine. 27 which has an inlet temperature that is a fourth intermediate temperature of the exchange line, higher than the third temperature, and then is gaseous sent to the medium pressure column 31. Preferably, the parts 19, 21 are mixed to form a single flow 23.
De manera diferente, además de las partes 19, 21, una parte 26 del aire a alta presión puede, eventualmente, proseguir su enfriamiento hasta el extremo frío de la línea de intercambio 11 y condensarse. A la salida del intercambiador, aquella será expandida en una válvula y enviada al sistema de columnas, por ejemplo, a la columna de media presión 31.In a different way, in addition to the parts 19, 21, a part 26 of the high-pressure air can eventually continue cooling to the cold end of the exchange line 11 and condense. At the exit of the exchanger, it will be expanded in a valve and sent to the column system, for example, to the medium pressure column 31.
La columna doble comprende una columna de media presión 31 y una columna de baja presión 33, conectadas térmicamente entre sí con caudales de reflujo 39, 41 de manera continua.The double column comprises a medium pressure column 31 and a low pressure column 33, thermally connected to each other with reflux flows 39, 41 continuously.
La columna de baja presión 33 produce un caudal de nitrógeno 43 que se recalienta en la línea de intercambio 11. Aquella produce igualmente oxígeno líquido 35 en depósito que es presurizado en 37 a una presión entre 10 y 16 bares y se vaporiza en la línea de intercambio para formar oxígeno gaseoso bajo presión.The low pressure column 33 produces a flow of nitrogen 43 which is reheated in the exchange line 11. It also produces liquid oxygen 35 in a tank that is pressurized in 37 at a pressure between 10 and 16 bar and vaporizes in the line of exchange to form gaseous oxygen under pressure.
Es concebible vaporizar oxígeno líquido a dos presiones diferentes de esta manera o vaporizar nitrógeno líquido o argón líquido, eventualmente, presurizado al mismo tiempo que el oxígeno líquido.It is conceivable to vaporize liquid oxygen at two different pressures in this way or vaporize liquid nitrogen or liquid argon, if necessary, pressurized at the same time as liquid oxygen.
En el caso en el que se vaporizan dos productos en la línea de intercambio (o un producto a dos niveles de presión diferentes), una parte del caudal 13 podrá proseguir su enfriamiento hasta el extremo frío del intercambiador y no ser sobrepresionado por el compresor de sobrepresión 25. Esta fracción de caudal se condensará. A la salida delIn the case where two products are vaporized in the exchange line (or a product at two different pressure levels), a part of the flow 13 may continue cooling to the cold end of the exchanger and not be overpressured by the compressor of overpressure 25. This fraction of flow will condense. At the exit of
33
intercambiador, aquella será expandida en una válvula y enviada al sistema de columnas, por ejemplo a la columna de media presión 31.exchanger, that will be expanded in a valve and sent to the column system, for example to the medium pressure column 31.
El compresor de sobrepresión 15 está accionado al menos en parte por una de las dos turbinas 17 o 25, y el compresor de sobrepresión 25 por la otra turbina 25 o 17. En cada caso, puede igualmente haber un motor o un 5 generador acoplado al compresor. Un dispositivo de disipación de energía 22, 24, por ejemplo un freno, preferiblemente un sistema de freno hidráulico, se integrará a al menos uno de los dos sistemas turbina/compresor 15/17, 25/27.The overpressure compressor 15 is driven at least in part by one of the two turbines 17 or 25, and the overpressure compressor 25 by the other turbine 25 or 17. In each case, there may also be a motor or a generator coupled to the compressor. An energy dissipation device 22, 24, for example a brake, preferably a hydraulic brake system, will be integrated into at least one of the two turbine / compressor systems 15/17, 25/27.
Claims (14)
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1152734A FR2973487B1 (en) | 2011-03-31 | 2011-03-31 | PROCESS AND APPARATUS FOR PRODUCING PRESSURIZED AIR GAS BY CRYOGENIC DISTILLATION |
| FR1152734 | 2011-03-31 | ||
| PCT/FR2012/050701 WO2012131277A2 (en) | 2011-03-31 | 2012-03-30 | Method for producing a gas from pressurised air by means of cryogenic distillation |
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| ES2675668T3 true ES2675668T3 (en) | 2018-07-11 |
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| ES12717421.7T Active ES2675668T3 (en) | 2011-03-31 | 2012-03-30 | Production process of a pressurized air gas by cryogenic distillation |
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| EP (1) | EP2691718B1 (en) |
| CN (1) | CN103827613B (en) |
| ES (1) | ES2675668T3 (en) |
| FR (1) | FR2973487B1 (en) |
| TR (1) | TR201808938T4 (en) |
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| US20130255313A1 (en) * | 2012-03-29 | 2013-10-03 | Bao Ha | Process for the separation of air by cryogenic distillation |
| EP3027988A2 (en) * | 2013-08-02 | 2016-06-08 | Linde Aktiengesellschaft | Method and device for producing compressed nitrogen |
| EP2963369B1 (en) * | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
| EP2963371B1 (en) * | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for creating a pressurised gas product by the cryogenic decomposition of air |
| EP3101374A3 (en) * | 2015-06-03 | 2017-01-18 | Linde Aktiengesellschaft | Method and installation for cryogenic decomposition of air |
| EP3290843A3 (en) * | 2016-07-12 | 2018-06-13 | Linde Aktiengesellschaft | Method and device for extracting pressurised nitrogen and pressurised nitrogen by cryogenic decomposition of air |
| EP3936192A4 (en) | 2019-03-06 | 2022-11-16 | Daiichi Sankyo Company, Limited | Pyrrolopyrazole derivative |
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| JP2909678B2 (en) * | 1991-03-11 | 1999-06-23 | レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Method and apparatus for producing gaseous oxygen under pressure |
| US5475980A (en) * | 1993-12-30 | 1995-12-19 | L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude | Process and installation for production of high pressure gaseous fluid |
| US6626008B1 (en) * | 2002-12-11 | 2003-09-30 | Praxair Technology, Inc. | Cold compression cryogenic rectification system for producing low purity oxygen |
| FR2854682B1 (en) * | 2003-05-05 | 2005-06-17 | Air Liquide | METHOD AND INSTALLATION OF AIR SEPARATION BY CRYOGENIC DISTILLATION |
| US6962062B2 (en) * | 2003-12-10 | 2005-11-08 | L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Proédés Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
| US7272954B2 (en) * | 2004-07-14 | 2007-09-25 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Proceded Georges Claude | Low temperature air separation process for producing pressurized gaseous product |
| DE102006012241A1 (en) * | 2006-03-15 | 2007-09-20 | Linde Ag | Method and apparatus for the cryogenic separation of air |
| US8020408B2 (en) * | 2006-12-06 | 2011-09-20 | Praxair Technology, Inc. | Separation method and apparatus |
| CN101779092A (en) * | 2007-08-10 | 2010-07-14 | 乔治洛德方法研究和开发液化空气有限公司 | Process and apparatus for the separation of air by cryogenic distillation |
| DE102009048456A1 (en) * | 2009-09-21 | 2011-03-31 | Linde Aktiengesellschaft | Method and apparatus for the cryogenic separation of air |
| US20130255313A1 (en) * | 2012-03-29 | 2013-10-03 | Bao Ha | Process for the separation of air by cryogenic distillation |
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| US20140007617A1 (en) | 2014-01-09 |
| TR201808938T4 (en) | 2018-07-23 |
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| EP2691718B1 (en) | 2018-05-02 |
| CN103827613B (en) | 2016-03-16 |
| FR2973487B1 (en) | 2018-01-26 |
| WO2012131277A2 (en) | 2012-10-04 |
| CN103827613A (en) | 2014-05-28 |
| WO2012131277A3 (en) | 2015-08-20 |
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