EP0641983A1 - Process and installation for the production of gaseous oxygen and/or nitrogen under pressure - Google Patents

Process and installation for the production of gaseous oxygen and/or nitrogen under pressure Download PDF

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Publication number
EP0641983A1
EP0641983A1 EP94401839A EP94401839A EP0641983A1 EP 0641983 A1 EP0641983 A1 EP 0641983A1 EP 94401839 A EP94401839 A EP 94401839A EP 94401839 A EP94401839 A EP 94401839A EP 0641983 A1 EP0641983 A1 EP 0641983A1
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EP
European Patent Office
Prior art keywords
pressure
air
column
turbine
heat exchange
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Granted
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EP94401839A
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German (de)
French (fr)
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EP0641983B1 (en
Inventor
Alain Guillard
Norbert Rieth
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP0641983A1 publication Critical patent/EP0641983A1/en
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air

Definitions

  • the invention aims to allow a reduction in the production of liquid for a given production capacity of oxygen and / or nitrogen gas under pressure, without increasing the specific energy of each production.
  • the subject of the invention is a method of the aforementioned type, characterized in that said part of the air is only released to an intermediate pressure, the turbined air is partially heated, then it is expanded in a second turbine up to medium pressure and it is introduced into the medium pressure column.
  • the invention also relates to an installation intended for the implementation of such a method.
  • This installation of the type comprising a double distillation column comprising a low pressure column operating under a pressure known as low pressure, and a medium pressure column operating under a pressure known as medium pressure; compression means for bringing all of the air to be distilled to at least one high pressure much higher than the medium pressure, these means comprising a main air compressor; means for withdrawing from the double column and pumping at least one liquid product resulting from the distillation; a heat exchange line bringing the air and said liquid product into heat exchange relationship; and an expansion turbine for part of this air, the intake of this turbine being connected to an intermediate point of the heat exchange line, is characterized in that the heat exchange line comprises partial heating passages, the inlet of which is connected to the exhaust of said turbine, and in that the installation includes a second expansion turbine whose inlet is connected to the outlet of these heating passages and whose exhaust is connected to the medium pressure column.
  • the installation shown in the drawing is intended to produce gaseous oxygen at a high pressure of approximately 10 to 100 bars, liquid oxygen and liquid nitrogen.
  • This installation essentially comprises: a main air compressor 1; a pre-cooler 2; an adsorption purification device 3; a blower-turbine assembly comprising a blower 4 and two turbines 5, 6 whose wheels are fixed on the same shaft; an atmospheric or water cooler 7 for the fan; a heat exchange line 8; a double distillation column 9 comprising a medium pressure column 10 and a low pressure column 11 coupled by a vaporizer-condenser 12 which brings the nitrogen at the top of column 10 into heat exchange relationship and liquid oxygen from the bottom of column 11; a liquid oxygen pump 13; a storage 14 of liquid oxygen at atmospheric pressure; a storage 15 of liquid nitrogen at atmospheric pressure; a separator pot 16; and a sub-cooler 17.
  • column 11 is under a pressure slightly higher than atmospheric pressure and column 10 under the corresponding pressure of approximately 5 to 6 bars.
  • All of the air to be distilled is compressed in 1, pre-cooled in 2 to + 5 to + 20 ° C, purified in water and in CO2 in 3 and boosted in 4 at high pressure. After pre-cooling in 7 and then partial cooling in passages 18 of the heat exchange line to an intermediate temperature T1, part of the air under high pressure continues to cool in passages 19 of the heat line. heat exchange, is liquefied and then divided into two fractions. Each fraction is expanded in a respective expansion valve 20, 21, then introduced into the respective column 10, 11.
  • T1 can be chosen to be around 10 ° C lower than the oxygen vaporization temperature, and T2 close to the knee for liquefying air under high pressure, this knee being below the vaporization temperature of oxygen and also below T1.
  • Liquid oxygen is withdrawn from the tank of column 11. A fraction goes directly to storage 15, via a pipe 24, while the rest is brought by pump 13 to the desired high production pressure, then vaporized and reheated at ambient temperature in passages 25 of the heat exchange line before being recovered via a pipe 26.
  • liquid nitrogen at medium pressure drawn off at the top of column 10 is sub-cooled at 17, expanded at atmospheric pressure in an expansion valve 27, and introduced into the separator pot 16.
  • the phase liquid is sent to storage 15, while the vapor phase is combined with impure nitrogen at the head of column 11, then the mixture is heated at 17 then in passages 28 of the heat exchange line and discharged from the installation as WN2 waste gas via line 29.
  • the invention also applies to the production of nitrogen gas under high pressure, brought by a pump (not shown) to the desired high pressure and then vaporized in the heat exchange line, and / or to the production of oxygen. and / or nitrogen under several pressures, using several high air pressures.

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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

In this process for producing gaseous oxygen and/or nitrogen under pressure by distillation of air in a double column (9), pumping (at 13) of at least one liquid product withdrawn from the vessel of the low-pressure column (11), and vaporisation (at 8) of the compressed liquid product by heat exchange with air compressed to a high air pressure, all of the air to be distilled is compressed to the high air pressure and the excess fraction of this air is expanded in two series turbines (5, 6) to the pressure of the medium-pressure column (10), the air being partially heated (at 22) between the two turbines. <IMAGE>

Description

La présente invention est relative à un procédé de production d'oxygène gazeux et/ou d'azote gazeux sous pression, du type dans lequel :

  • on distille de l'air dans une double colonne de distillation comprenant une colonne basse pression fonctionnant sous une pression dite basse pression, et une colonne moyenne pression fonctionnant sous une pression dite moyenne pression;
  • on comprime la totalité de l'air à distiller jusqu'à au moins une haute pression d'air nettement supérieure à la moyenne pression;
  • on refroidit l'air comprimé jusqu'à une température intermédiaire, et on en détend une partie dans une turbine avant de l'introduire dans la colonne moyenne pression;
  • on liquéfie l'air non turbiné, puis on l'introduit, après détente, dans la double colonne; et
  • on amène au moins un produit liquide soutiré de la double colonne à la pression de production, et on vaporise ce produit liquide par échange de chaleur avec l'air, la température de liquéfaction de l'air étant inférieure à la température de vaporisation du produit liquide.
The present invention relates to a process for producing gaseous oxygen and / or nitrogen gas under pressure, of the type in which:
  • air is distilled in a double distillation column comprising a low pressure column operating under a pressure known as low pressure, and a medium pressure column operating under a pressure known as medium pressure;
  • all the air to be distilled is compressed to at least one high air pressure which is clearly higher than the medium pressure;
  • the compressed air is cooled to an intermediate temperature, and part of it is expanded in a turbine before being introduced into the medium pressure column;
  • the non-turbinated air is liquefied, then introduced, after expansion, into the double column; and
  • at least one liquid product withdrawn from the double column is brought to production pressure, and this liquid product is vaporized by heat exchange with the air, the air liquefaction temperature being lower than the product vaporization temperature liquid.

Les pressions dont il est question dans le présent mémoire sont des pressions absolues. De plus, l'expression "liquéfaction" doit être entendu au sens large, c'est-à-dire incluant la pseudo-liquéfaction dans le cas de pressions supercritiques.The pressures discussed in this brief are absolute pressures. In addition, the expression "liquefaction" must be understood in the broad sense, that is to say including pseudo-liquefaction in the case of supercritical pressures.

Un procédé du type ci-dessus est décrit dans le FR-A-2 674 011. Dans ce procédé, la production gazeuse sous pression s'accompagne inévitablement d'une production de liquide, laquelle n'est pas souhaitable dans toutes les applications industrielles.A process of the above type is described in FR-A-2 674 011. In this process, gaseous production under pressure is inevitably accompanied by production of liquid, which is not desirable in all industrial applications .

L'invention a pour but de permettre une réduction de la production de liquide pour une capacité de production donnée d'oxygène et/ou d'azote gazeux sous pression, ce sans augmentation de l'énergie spécifique de chaque production.The invention aims to allow a reduction in the production of liquid for a given production capacity of oxygen and / or nitrogen gas under pressure, without increasing the specific energy of each production.

A cet effet, l'invention a pour objet un procédé du type précité, caractérisé en ce qu'on ne détend ladite partie de l'air que jusqu'à une pression intermédiaire, on réchauffe partiellement l'air turbiné, puis on le détend dans une seconde turbine jusqu'à la moyenne pression et on l'introduit dans la colonne moyenne pression.To this end, the subject of the invention is a method of the aforementioned type, characterized in that said part of the air is only released to an intermediate pressure, the turbined air is partially heated, then it is expanded in a second turbine up to medium pressure and it is introduced into the medium pressure column.

Dans des modes de mise en oeuvre de ce procédé :

  • ladite température intermédiaire est inférieure, notamment d'environ 10°C, à la température de vaporisation dudit produit liquide;
  • la température d'admission de la seconde turbine est voisine du genou de liquéfaction de l'air.
In embodiments of this process:
  • said intermediate temperature is lower, in particular about 10 ° C, than the vaporization temperature of said liquid product;
  • the inlet temperature of the second turbine is close to the knee for liquefying the air.

L'invention a également pour objet une installation destinée à la mise en oeuvre d'un tel procédé. Cette installation, du type comprenant une double colonne de distillation comprenant une colonne basse pression fonctionnant sous une pression dite basse pression, et une colonne moyenne pression fonctionnant sous une pression dite moyenne pression; des moyens de compression pour amener la totalité de l'air à distiller à au moins une haute pression nettement supérieure à la moyenne pression, ces moyens comprenant un compresseur principal d'air; des moyens de soutirage de la double colonne et de pompage d'au moins un produit liquide résultant de la distillation; une ligne d'échange thermique mettant en relation d'échange thermique l'air et ledit produit liquide; et une turbine de détente d'une partie de cet air, l'admission de cette turbine étant reliée à un point intermédiaire de la ligne d'échange thermique, est caractérisée en ce que la ligne d'échange thermique comprend des passages de réchauffement partiel dont l'entrée est reliée à l'échappement de ladite turbine, et en ce que l'installation comprend une seconde turbine de détente dont l'admission est reliée à la sortie de ces passages de réchauffement et dont l'échappement est relié à la colonne moyenne pression.The invention also relates to an installation intended for the implementation of such a method. This installation, of the type comprising a double distillation column comprising a low pressure column operating under a pressure known as low pressure, and a medium pressure column operating under a pressure known as medium pressure; compression means for bringing all of the air to be distilled to at least one high pressure much higher than the medium pressure, these means comprising a main air compressor; means for withdrawing from the double column and pumping at least one liquid product resulting from the distillation; a heat exchange line bringing the air and said liquid product into heat exchange relationship; and an expansion turbine for part of this air, the intake of this turbine being connected to an intermediate point of the heat exchange line, is characterized in that the heat exchange line comprises partial heating passages, the inlet of which is connected to the exhaust of said turbine, and in that the installation includes a second expansion turbine whose inlet is connected to the outlet of these heating passages and whose exhaust is connected to the medium pressure column.

Suivant d'autres caractéristiques de cette installation :

  • les deux turbines sont calées sur le même arbre;
  • l'arbre des deux turbines est solidaire de la roue d'une soufflante de surpression de l'air issu du compresseur principal d'air.
According to other characteristics of this installation:
  • the two turbines are set on the same shaft;
  • the shaft of the two turbines is integral with the wheel of an air pressure blower from the main air compressor.

Un exemple de mise en oeuvre de l'invention va maintenant être décrit en regard du dessin annexé, dont la figure unique représente schématiquement une installation de production d'oxygène gazeux sous pression conforme à l'invention.An example of implementation of the invention will now be described with reference to the accompanying drawing, the single figure of which schematically represents an installation for producing gaseous oxygen under pressure in accordance with the invention.

L'installation représentée au dessin est destinée à produire de l'oxygène gazeux sous une haute pression de 10 à 100 bars environ, de l'oxygène liquide et de l'azote liquide.The installation shown in the drawing is intended to produce gaseous oxygen at a high pressure of approximately 10 to 100 bars, liquid oxygen and liquid nitrogen.

Cette installation comprend essentiellement: un compresseur principal d'air 1; un pré-refroidisseur 2; un appareil 3 d'épuration par adsorption; un ensemble soufflante-turbines comprenant une soufflante 4 et deux turbines 5, 6 dont les roues sont calées sur le même arbre; un réfrigérant atmosphérique ou à eau 7 pour la soufflante; une ligne d'échange thermique 8; une double colonne de distillation 9 comprenant une colonne moyenne pression 10 et une colonne basse pression 11 couplées par un vaporiseur- condenseur 12 qui met en relation d'échange thermique l'azote de tête de la colonne 10 et l'oxygène liquide de cuve de la colonne 11; une pompe d'oxygène liquide 13; un stockage 14 d'oxygène liquide à la pression atmosphérique; un stockage 15 d'azote liquide à la pression atmosphérique; un pot séparateur 16; et un sous-refroidisseur 17.This installation essentially comprises: a main air compressor 1; a pre-cooler 2; an adsorption purification device 3; a blower-turbine assembly comprising a blower 4 and two turbines 5, 6 whose wheels are fixed on the same shaft; an atmospheric or water cooler 7 for the fan; a heat exchange line 8; a double distillation column 9 comprising a medium pressure column 10 and a low pressure column 11 coupled by a vaporizer-condenser 12 which brings the nitrogen at the top of column 10 into heat exchange relationship and liquid oxygen from the bottom of column 11; a liquid oxygen pump 13; a storage 14 of liquid oxygen at atmospheric pressure; a storage 15 of liquid nitrogen at atmospheric pressure; a separator pot 16; and a sub-cooler 17.

En fonctionnement, la colonne 11 est sous une pression légèrement supérieure à la pression atmosphérique et la colonne 10 sous la pression correspondante de 5 à 6 bars environ.In operation, column 11 is under a pressure slightly higher than atmospheric pressure and column 10 under the corresponding pressure of approximately 5 to 6 bars.

La totalité de l'air à distiller est comprimé en 1, pré-refroidi en 2 vers + 5 à + 20°C, épuré en eau et en C02 en 3 et surpressé en 4 à la haute pression. Après pré-refroidissement en 7 puis refroidissement partiel dans des passages 18 de la ligne d'échange thermique jusqu'à une température intermédiaire T1, une partie de l'air sous la haute pression poursuit son refroidissement dans des passages 19 de la ligne d'échange thermique, est liquéfiée puis divisée en deux fractions. Chaque fraction est détendue dans une vanne de détente respective 20, 21, puis introduite dans la colonne 10, 11 respective.All of the air to be distilled is compressed in 1, pre-cooled in 2 to + 5 to + 20 ° C, purified in water and in CO2 in 3 and boosted in 4 at high pressure. After pre-cooling in 7 and then partial cooling in passages 18 of the heat exchange line to an intermediate temperature T1, part of the air under high pressure continues to cool in passages 19 of the heat line. heat exchange, is liquefied and then divided into two fractions. Each fraction is expanded in a respective expansion valve 20, 21, then introduced into the respective column 10, 11.

A la température T1, le reste de l'air sous la haute pression est sorti de la ligne d'échange thermique, turbiné en 5 à une pression intermédiaire, réintroduit dans la ligne d'échange thermique, réchauffé partiellement dans des passages 22 de celle-ci, jusqu'à une température intermédiaire T2 qui peut être ou non égale à T1, sorti de nouveau de la ligne d'échange thermique, turbiné en 6 à la moyenne pression et introduit en cuve de la colonne 10.At temperature T1, the rest of the air under high pressure is removed from the heat exchange line, turbinated at 5 at an intermediate pressure, reintroduced into the heat exchange line, partially reheated in passages 22 of that here, up to an intermediate temperature T2 which may or may not be equal to T1, again removed from the heat exchange line, turbinated at 6 at medium pressure and introduced into the tank of column 10.

On peut notamment choisir T1 inférieure d'environ 10°C à la température de vaporisation de l'oxygène, et T2 voisine du genou de liquéfaction de l'air sous la haute pression, ce genou étant au-dessous de la température de vaporisation de l'oxygène et également au-dessous de T1.In particular, T1 can be chosen to be around 10 ° C lower than the oxygen vaporization temperature, and T2 close to the knee for liquefying air under high pressure, this knee being below the vaporization temperature of oxygen and also below T1.

De façon habituelle, du "liquide riche" (air enrichi en oxygène) soutiré en cuve de la colonne 10 et du "liquide pauvre" (azote à peu près pur) soutiré dans la région supérieure de cette colonne sont, après sous-refroidissement en 17 et détente dans des vannes de détente respectives 22 et 23, introduits à un niveau intermédiaire et en tête, respectivement, de la colonne 11.Usually, "rich liquid" (oxygen-enriched air) withdrawn from the tank of column 10 and "lean liquid" (approximately pure nitrogen) withdrawn in the upper region of this column are, after sub-cooling in 17 and expansion in respective expansion valves 22 and 23, introduced at an intermediate level and at the head, respectively, of column 11.

De l'oxygène liquide est soutiré en cuve de la colonne 11. Une fraction va directement dans le stockage 15, via une conduite 24, tandis que le reste est amené par la pompe 13 à la haute pression de production désirée, puis vaporisé et réchauffé à la température ambiante dans des passages 25 de la ligne d'échange thermique avant d'être récupéré via une conduite 26.Liquid oxygen is withdrawn from the tank of column 11. A fraction goes directly to storage 15, via a pipe 24, while the rest is brought by pump 13 to the desired high production pressure, then vaporized and reheated at ambient temperature in passages 25 of the heat exchange line before being recovered via a pipe 26.

Par ailleurs, de l'azote liquide sous la moyenne pression, soutiré en tête de la colonne 10, est sous-refroidi en 17, détendu à la pression atmosphérique dans une vanne de détente 27, et introduit dans le pot séparateur 16. La phase liquide est envoyée dans le stockage 15, tandis que la phase vapeur est réunie à l'azote impur de tête de la colonne 11, puis le mélange est réchauffé en 17 puis dans des passages 28 de la ligne d'échange thermique et évacué de l'installation en tant que gaz résiduaire WN2 via une conduite 29.Furthermore, liquid nitrogen at medium pressure, drawn off at the top of column 10, is sub-cooled at 17, expanded at atmospheric pressure in an expansion valve 27, and introduced into the separator pot 16. The phase liquid is sent to storage 15, while the vapor phase is combined with impure nitrogen at the head of column 11, then the mixture is heated at 17 then in passages 28 of the heat exchange line and discharged from the installation as WN2 waste gas via line 29.

Des calculs effectués sur la base d'une production de 248 tonnes par jour d'oxygène à 99,5% de pureté sous 40 bars, ont montré qu'on pouvait abaisser la haute pression d'air à 25,5 bars, contre 30 bars pour la configuration à une seule turbine du FR-A-2 674 011 précité. Dans les mêmes conditions, le ratio liquide/capacité de séparation en oxygène passe de 30% à 22%, et l'énergie spécifique de chaque production reste inchangée.Calculations made on the basis of a production of 248 tonnes per day of oxygen at 99.5% purity under 40 bars, showed that the high air pressure could be lowered to 25.5 bars, against 30 bars for the configuration with a single turbine of the aforementioned FR-A-2 674 011. Under the same conditions, the liquid / oxygen separation capacity ratio goes from 30% to 22%, and the specific energy of each production remains unchanged.

L'invention s'applique également à la production d'azote gazeux sous haute pression, porté par une pompe (non représentée) à la haute pression désirée puis vaporisé dans la ligne d'échange thermique, et/ou à la production d'oxygène et/ou d'azote sous plusieurs pressions, en utilisant plusieurs hautes pressions d'air.The invention also applies to the production of nitrogen gas under high pressure, brought by a pump (not shown) to the desired high pressure and then vaporized in the heat exchange line, and / or to the production of oxygen. and / or nitrogen under several pressures, using several high air pressures.

Claims (6)

1 - Procédé de production d'oxygène gazeux et/ou d'azote gazeux sous pression, du type dans lequel: - on distille de l'air dans une double colonne de distillation (9) comprenant une colonne basse pression (11) fonctionnant sous une pression dite basse pression, et une colonne moyenne pression (10) fonctionnant sous une pression dite moyenne pression; - on comprime (en 1, 4) la totalité de l'air à distiller jusqu'à au moins une haute pression d'air nettement supérieure à la moyenne pression; - on refroidit l'air comprimé jusqu'à une température intermédiaire (T1), et on en détend une partie dans une turbine (5) avant de l'introduire dans la colonne moyenne pression (10); - on liquéfie l'air non turbiné, puis on l'introduit, après détente (en 20, 21), dans la double colonne; et - on amène (en 13) au moins un produit liquide soutiré de la double colonne à la pression de production, et on vaporise (en 8) ce produit liquide par échange de chaleur avec l'air, la température de liquéfaction de l'air étant inférieure à la température de vaporisation du produit liquide, caractérisé en ce qu'on ne détend ladite partie de l'air que jusqu'à une pression intermédiaire, on réchauffe partiellement (en 22) l'air turbiné, puis on le détend dans une seconde turbine (6) jusqu'à la moyenne pression et on l'introduit dans la colonne moyenne pression (10). 1 - Process for the production of gaseous oxygen and / or nitrogen gas under pressure, of the type in which: - Air is distilled in a double distillation column (9) comprising a low pressure column (11) operating under a pressure called low pressure, and a medium pressure column (10) operating under a pressure called medium pressure; - It compresses (in 1, 4) all of the air to be distilled to at least a high air pressure significantly higher than the medium pressure; - The compressed air is cooled to an intermediate temperature (T1), and part of it is expanded in a turbine (5) before introducing it into the medium pressure column (10); - the non-turbinated air is liquefied, then introduced, after expansion (in 20, 21), into the double column; and - one brings (at 13) at least one liquid product withdrawn from the double column to the production pressure, and one vaporizes (at 8) this liquid product by heat exchange with air, the air liquefaction temperature being lower than the vaporization temperature of the liquid product, characterized in that said part of the air is only expanded to an intermediate pressure, the turbinated air is partially heated (at 22), then it is expanded in a second turbine (6) to the mean pressure and it is introduced into the medium pressure column (10). 2 - Procédé suivant la revendication 1, caractérisé en ce que ladite température intermédiaire (T1) est inférieure, notamment d'environ 10°C, à la température de vaporisation dudit produit liquide. 2 - Process according to claim 1, characterized in that said intermediate temperature (T1) is lower, in particular by about 10 ° C, than the vaporization temperature of said liquid product. 3 - Procédé suivant la revendication 1 ou 2, caractérisé en ce que la température (T2) d'admission de la seconde turbine (6) est voisine du genou de liquéfaction de l'air. 3 - Process according to claim 1 or 2, characterized in that the intake temperature (T2) of the second turbine (6) is close to the knee for liquefying the air. 4 - Installation de production d'oxygène gazeux et/ou d'azote gazeux sous pression, du type comprenant une double colonne de distillation (9) comprenant une colonne basse pression (11) fonctionnant sous une pression dite basse pression, et une colonne moyenne pression (10) fonctionnant sous une pression dite moyenne pression, ces moyens comprenant un compresseur principal d'air (1); des moyens de compression (1, 4) pour amener la totalité de l'air à distiller à au moins une haute pression nettement supérieure à la moyenne pression; des moyens (13) de soutirage de la double colonne et de pompage d'au moins un produit liquide résultant de la distillation; une ligne d'échange thermique (8) mettant en relation d'échange thermique l'air et ledit produit liquide; et une turbine (5) de détente d'une partie de cet air, l'admission de cette turbine étant reliée à un point intermédiaire de la ligne d'échange thermique, caractérisée en ce que la ligne d'échange thermique (8) comprend des passages de réchauffement partiel (22) dont l'entrée est reliée à l'échappement de ladite turbine (5), et en ce que l'installation comprend une seconde turbine de détente (6) dont l'admission est reliée à la sortie de ces passages de réchauffement et dont l'échappement est relié à la colonne moyenne pression (10). 4 - Installation for producing gaseous oxygen and / or nitrogen gas under pressure, of the type comprising a double distillation column (9) comprising a low pressure column (11) operating under a pressure known as low pressure, and a medium column pressure (10) operating under a so-called medium pressure, these means comprising a main air compressor (1); compression means (1, 4) for bringing all of the air to be distilled to at least one high pressure significantly higher than the medium pressure; means (13) for withdrawing from the double column and pumping at least one liquid product resulting from the distillation; a heat exchange line (8) bringing the air and said liquid product into heat exchange relationship; and a turbine (5) for expanding part of this air, the intake of this turbine being connected to an intermediate point of the heat exchange line, characterized in that the heat exchange line (8) comprises partial heating passages (22), the inlet of which is connected to the exhaust of said turbine (5), and in that the installation comprises a second expansion turbine (6), the inlet of which is connected to the outlet of these heating passages and the exhaust of which is connected to the medium pressure column (10). 5 - Installation suivant la revendication 4, caractérisée en ce que les deux turbines (5, 6) sont calées sur le même arbre. 5 - Installation according to claim 4, characterized in that the two turbines (5, 6) are wedged on the same shaft. 6 - Installation suivant la revendication 5, caractérisée en ce que l'arbre des deux turbines (5, 6) est solidaire de la roue d'une soufflante (4) de surpression de l'air issu du compresseur principal d'air (1). 6 - Installation according to claim 5, characterized in that the shaft of the two turbines (5, 6) is integral with the wheel of a blower (4) for overpressure of the air from the main air compressor (1 ).
EP94401839A 1993-09-01 1994-08-10 Process and installation for the production of gaseous oxygen and/or nitrogen under pressure Expired - Lifetime EP0641983B1 (en)

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FR9310417 1993-09-01
FR9310417A FR2709537B1 (en) 1993-09-01 1993-09-01 Process and installation for producing oxygen and / or nitrogen gas under pressure.

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JP (1) JPH07151458A (en)
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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2776760A1 (en) * 1998-03-31 1999-10-01 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
EP0646755B2 (en) † 1993-09-15 2001-11-28 Air Products And Chemicals, Inc. Cryogenic air separation process and apparatus producing elevated pressure nitrogen by pumped liquid nitrogen
FR2928446A1 (en) * 2008-03-10 2009-09-11 Air Liquide METHOD FOR MODIFYING AN AIR SEPARATION APPARATUS BY CRYOGENIC DISTILLATION
CN104406365A (en) * 2014-11-27 2015-03-11 苏州制氧机股份有限公司 Double-expander medium-pressure liquid device

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2730172B1 (en) * 1995-02-07 1997-03-21 Air Liquide METHOD AND APPARATUS FOR MONITORING THE OPERATION OF AN AIR SEPARATION INSTALLATION
US5758515A (en) * 1997-05-08 1998-06-02 Praxair Technology, Inc. Cryogenic air separation with warm turbine recycle
US5979440A (en) * 1997-06-16 1999-11-09 Sequal Technologies, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
FR2795495B1 (en) * 1999-06-23 2001-09-14 Air Liquide PROCESS AND PLANT FOR SEPARATING A GASEOUS MIXTURE BY CRYOGENIC DISTILLATION
JP4594360B2 (en) * 2007-08-27 2010-12-08 神鋼エア・ウォーター・クライオプラント株式会社 Cryogenic air liquefaction separation device and operation method thereof
EP2464937A2 (en) * 2009-08-11 2012-06-20 Linde AG Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air
JP6546504B2 (en) * 2015-10-20 2019-07-17 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 Oxygen production system and oxygen production method

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2674011A1 (en) * 1991-03-11 1992-09-18 Grenier Maurice Method and installation for producing gaseous oxygen under pressure

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2652409A1 (en) * 1989-09-25 1991-03-29 Air Liquide REFRIGERANT PRODUCTION PROCESS, CORRESPONDING REFRIGERANT CYCLE AND THEIR APPLICATION TO AIR DISTILLATION.
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
US5365741A (en) * 1993-05-13 1994-11-22 Praxair Technology, Inc. Cryogenic rectification system with liquid oxygen boiler

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2674011A1 (en) * 1991-03-11 1992-09-18 Grenier Maurice Method and installation for producing gaseous oxygen under pressure

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0646755B2 (en) † 1993-09-15 2001-11-28 Air Products And Chemicals, Inc. Cryogenic air separation process and apparatus producing elevated pressure nitrogen by pumped liquid nitrogen
FR2776760A1 (en) * 1998-03-31 1999-10-01 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
US6463758B1 (en) 1998-03-31 2002-10-15 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for separating air by cryogenic distillation
DE19913907B4 (en) * 1998-03-31 2007-07-26 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and apparatus for separating air by cryogenic distillation
FR2928446A1 (en) * 2008-03-10 2009-09-11 Air Liquide METHOD FOR MODIFYING AN AIR SEPARATION APPARATUS BY CRYOGENIC DISTILLATION
CN104406365A (en) * 2014-11-27 2015-03-11 苏州制氧机股份有限公司 Double-expander medium-pressure liquid device

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ES2102790T3 (en) 1997-08-01
EP0641983B1 (en) 1997-04-16
CA2131120A1 (en) 1995-03-02
US5477689A (en) 1995-12-26
FR2709537B1 (en) 1995-10-13
FR2709537A1 (en) 1995-03-10
DE69402643D1 (en) 1997-05-22
CN1102701A (en) 1995-05-17
JPH07151458A (en) 1995-06-16
DE69402643T2 (en) 1997-10-02

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