FR2849172A1 - Improved air distillation process, for oxygen production, uses vaporized gas from storage for at least partial pressurization of adsorber ending regeneration phase - Google Patents

Improved air distillation process, for oxygen production, uses vaporized gas from storage for at least partial pressurization of adsorber ending regeneration phase Download PDF

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Publication number
FR2849172A1
FR2849172A1 FR0216141A FR0216141A FR2849172A1 FR 2849172 A1 FR2849172 A1 FR 2849172A1 FR 0216141 A FR0216141 A FR 0216141A FR 0216141 A FR0216141 A FR 0216141A FR 2849172 A1 FR2849172 A1 FR 2849172A1
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Prior art keywords
nitrogen
air
adsorber
column
liquid
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FR0216141A
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French (fr)
Inventor
Frederic Judas
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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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Priority to FR0216141A priority Critical patent/FR2849172A1/en
Publication of FR2849172A1 publication Critical patent/FR2849172A1/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being nitrogen
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Abstract

A gas (31) containing at least 78 mol% of nitrogen, produced by vaporization of liquid from a storage vessel (22), is used to at least partially pressurize the pressure swing adsorber (PSA) ending its regeneration phase. The liquid originates from the heat exchanger line (8) of from one (12, 14) of the system of columns. The gas containing 78 mol% nitrogen, used to pressurize each adsorber (7A, 7B), is at greater pressure than the high pressure of the adsorption phase (Pads). At least some of this gas is stored under a pressure below Pads. A part of the gas is air from the heat exchanger line (8). Some of this air is stored in liquid form, downstream of the exchanger line. Some of the gas used for pressurization is nitrogen from the head of the medium pressure column (12) and/or low pressure gas from the double column (10). The stored liquid vaporizes in the exchanger line (8) through heat exchange with air to be distilled, or in a dedicated vaporizer (30). An Independent claim is included for a corresponding plant.

Description

1-' 28491721- '2849172

La présente invention concerne un procédé de distillation d'air, notamment destiné à produire de l'oxygène, du type dans lequel l'air à distiller est préalablement épuré au moyen d'au moins deux adsorbeurs qui suivent chacun, en décalage, un cycle o se succèdent une phase d'adsorption, à une pression du cycle, et une phase de régénération se terminant par une pressurisation de 10 I'adsorbeur.  The present invention relates to an air distillation process, in particular intended for producing oxygen, of the type in which the air to be distilled is previously purified by means of at least two adsorbers which each follow, in offset, a cycle o there is an adsorption phase, at a cycle pressure, and a regeneration phase ending with a pressurization of the adsorber.

Elle concerne également une installation de mise en oeuvre d'un tel procédé.  It also relates to an installation for implementing such a method.

Les pressions dont il est question ici sont des pressions absolues.  The pressures we are talking about here are absolute pressures.

Dans ce type d'installation, la distillation de l'air, préalablement comprimé par un appareil de compression, s'effectue par voie cryogénique et nécessite donc 15 de purifier l'air afin d'en éliminer les constituants dont les températures de solidification sont supérieures à la température de distillation de l'air, à savoir principalement l'eau et le dioxyde de carbone L'objectif principal de la distillation de l'air est de fournir, sous forme liquide et/ou gazeuse, de l'oxygène Cette production d'oxygène engendre la coproduction de fluides à faible teneur en oxygène, tels que, 20 par exemple, de l'azote impur, dit azote résiduaire ou " waste ", et de l'azote à plus haute pureté, sous forme liquide ou gazeuse.  In this type of installation, the distillation of the air, previously compressed by a compression device, is carried out by cryogenic means and therefore requires the air to be purified in order to remove the constituents whose solidification temperatures are higher than the air distillation temperature, mainly water and carbon dioxide The main objective of air distillation is to provide, in liquid and / or gaseous form, oxygen This oxygen production leads to the co-production of fluids with low oxygen content, such as, for example, impure nitrogen, known as "waste nitrogen", and higher purity nitrogen, in liquid form or gas.

La purification de l'air à distiller est couramment effectuée par adsorption des constituants gênants, au moyen en général de deux bouteilles contenant des substances adsorbantes disposées en lit et fonctionnant en cycles alternés. 25 Pendant qu'une bouteille est en phase d'adsorption, c'est à dire qu'elle épure l'air devant être distillé, I'autre bouteille est en phase de régénération, c'est à dire qu'elle est balayée par un gaz de régénération sec, tel que l'azote résiduaire, désorbant les impuretés fixées sur l'adsorbant lors de sa phase d'adsorption précédente La régénération de l'adsorbant est d'autant plus efficace qu'elle est 30 appliquée à haute température et à une basse pression par rapport à celle maintenue pendant l'adsorption, ce qui oblige à pressuriser une bouteille terminant sa phase de régénération, afin de la remettre en condition de pression satisfaisante pour sa phase d'adsorption à venir.  The purification of the air to be distilled is commonly carried out by adsorption of the troublesome constituents, generally by means of two bottles containing adsorbent substances arranged in a bed and operating in alternating cycles. 25 While a bottle is in the adsorption phase, that is to say that it purifies the air to be distilled, the other bottle is in the regeneration phase, that is to say that it is swept by a dry regeneration gas, such as residual nitrogen, desorbing the impurities fixed on the adsorbent during its previous adsorption phase The regeneration of the adsorbent is all the more effective when it is applied at high temperature and at a low pressure relative to that maintained during adsorption, which requires pressurizing a bottle ending its regeneration phase, in order to return it to a satisfactory pressure condition for its future adsorption phase.

Pour cela, l'état de l'art consiste à prélever une fraction d'air épuré en sortie 35 de la bouteille en phase d'adsorption et de la détendre vers la bouteille en fin de phase régénération, afin d'augmenter la pression de cette dernière Pendant cette opération, il est cependant indispensable de maintenir constant le débit d'air à envoyer à la distillation afin d'éviter toute fluctuation d'alimentation de l'appareil de distillation et pour maintenir la production d'oxygène Aussi, pendant chaque 5 repressurisation, I'appareil de compression d'air doit fournir ce surplus d'air qui sert à la pressurisation.  For this, the state of the art consists in taking a fraction of purified air at the outlet 35 of the bottle in the adsorption phase and in relaxing it towards the bottle at the end of the regeneration phase, in order to increase the pressure of the latter During this operation, it is however essential to maintain constant the air flow to be sent to the distillation in order to avoid any fluctuation in the supply of the distillation apparatus and to maintain the production of oxygen Also, during each 5 repressurization, the air compression device must provide this excess air which is used for pressurization.

Cependant, ce débit d'air supplémentaire implique un surdimensionnement, et donc un surcot, de l'appareil de compression Il lui est en effet demandé de fournir un débit d'air comprimé supplémentaire de l'ordre de 5 % du débit d'air 10 nominal traité par la bouteille en adsorption (selon l'optimisation du cycle), pendant une durée de pressurisation de l'ordre de 15 minutes pour une bouteille de dimension courante.  However, this additional air flow implies an oversizing, and therefore an overload, of the compression device. It is in fact asked to provide an additional compressed air flow of the order of 5% of the air flow. 10 nominal treated by the bottle in adsorption (according to the optimization of the cycle), for a pressurization duration of the order of 15 minutes for a bottle of current size.

Par suite, en dehors de la durée de pressurisation, I'appareil de compression fonctionne au débit d'air nominal, c'est-à-dire celui qui correspond à la capacité de 15 séparation de l'appareil de séparation d'air.  As a result, apart from the pressurization time, the compression apparatus operates at the nominal air flow rate, that is to say that which corresponds to the separation capacity of the air separation apparatus.

Le but de l'invention est d'éviter cet inconvénient en réduisant, voire en supprimant, I'augmentation du débit d'air à comprimer pour fournir le gaz supplémentaire nécessaire à la pressurisation des bouteilles d'adsorbant.  The object of the invention is to avoid this drawback by reducing, or even eliminating, the increase in the air flow rate to be compressed in order to supply the additional gas necessary for the pressurization of the bottles of adsorbent.

A cet effet, I'invention a pour objet un procédé du type précité, dans lequel 20 on utilise un gaz contenant au moins 78 % mol d' azote, produit par vaporisation d'un liquide stocké dans un stockage pour pressuriser, au moins partiellement, I'adsorbeur terminant sa phase de régénération.  To this end, the invention relates to a process of the aforementioned type, in which a gas containing at least 78% mol of nitrogen is used, produced by vaporization of a liquid stored in a storage to pressurize, at least partially , The adsorber ending its regeneration phase.

Suivant d'autres caractéristiques de ce procédé, prises isolément ou selon les combinaisons techniquement possibles: le liquide provient de la ligne d'échange ou d'une colonne du système de colonnes. le gaz contenant au moins 78 % mol d'azote utilisé pour pressuriser chaque adsorbeur est à une pression supérieure à la haute pression de la phase d'adsorption. une partie au moins du gaz contenant au moins 78 % mol d'azote utilisé pour pressuriser chaque adsorbeur est stockée sous une pression de stockage inférieure à la haute pression de la phase d'adsorption.  According to other characteristics of this process, taken in isolation or in technically possible combinations: the liquid comes from the exchange line or from a column of the column system. the gas containing at least 78 mol% of nitrogen used to pressurize each adsorber is at a pressure higher than the high pressure of the adsorption phase. at least part of the gas containing at least 78 mol% of nitrogen used to pressurize each adsorber is stored under a storage pressure lower than the high pressure of the adsorption phase.

une partie au moins du gaz contenant au moins 78 % mol d'azote utilisée pour pressuriser chaque adsorbeur est de l'air et provient de la ligne d'échange.  at least part of the gas containing at least 78 mol% of nitrogen used to pressurize each adsorber is air and comes from the exchange line.

une partie au moins de l'air utilisé pour pressuriser chaque adsorbeur est stockée sous forme liquide en aval de la ligne d'échange.  at least part of the air used to pressurize each adsorber is stored in liquid form downstream of the exchange line.

-une partie au moins le gaz contenant au moins 78 % mol d'azote utilisé pour pressuriser chaque adsorbeur est de l'azote de tête de la colonne moyenne pression et/ ou basse pression d'une double colonne.  at least part of the gas containing at least 78% mol of nitrogen used to pressurize each adsorber is nitrogen from the top of the medium pressure and / or low pressure column of a double column.

le liquide stocké se vaporise dans la ligne d'échange de l'appareil par échange de chaleur avec l'air à distiller ou dans un vaporiseur dédié.  the stored liquid is vaporized in the exchange line of the device by heat exchange with the air to be distilled or in a dedicated vaporizer.

L'invention a également pour objet un procédé de distillation d'air, notamment destiné à produire de l'oxygène, du type dans lequel l'air à distiller est 10 préalablement épuré au moyen d'au moins deux adsorbeurs qui suivent chacun, en décalage, un cycle o se succèdent une phase d'adsorption, à une haute pression du cycle, et une phase de régénération se terminant par une repressurisation de l'adsorbeur, I'air épuré est refroidi dans une ligne d'échange et ensuite envoyé à une colonne de distillation d'un système de colonnes et des 15 fluides enrichis en oxygène et en azote sont soutirés d'une colonne du système de colonnes caractérisé en ce qu'on utilise un gaz contenant au moins 78 % mol.  The invention also relates to a process for the distillation of air, in particular intended for producing oxygen, of the type in which the air to be distilled is previously purified by means of at least two adsorbers which each follow, in offset, a cycle where an adsorption phase follows, at a high pressure of the cycle, and a regeneration phase ending with a repressurization of the adsorber, the purified air is cooled in an exchange line and then sent from a distillation column of a column system and fluids enriched in oxygen and nitrogen are withdrawn from a column of the column system characterized in that a gas containing at least 78 mol% is used.

d'azote, provenant un réseau extérieur, pour pressuriser, au moins partiellement, I'adsorbeur terminant sa phase de régénération.  nitrogen, coming from an external network, to pressurize, at least partially, the adsorber ending its regeneration phase.

L'invention a également pour objet une installation de distillation d'air, 20 notamment destinée à produire de l'oxygène, du type comportant un appareil d'épuration par adsorption d'air à distiller qui comprend au moins deux adsorbeurs qui suivent chacun, en décalage, un cycle o se succèdent une phase d'adsorption, à une haute pression du cycle (Pads), et une phase de régénération se terminant par une pressurisation de l'adsorbeur, et un appareil de distillation de l'air épuré 25 comprenant une ligne d'échange et un système de colonnes, caractérisée en ce qu'elle comporte des moyens de stockage d'un liquide contenant au moins 78 % mol d'azote, des moyens de vaporisation du liquide contenant au moins 78 % mol.  The subject of the invention is also an air distillation installation, in particular intended for producing oxygen, of the type comprising an air purification device by adsorption of air to be distilled which comprises at least two adsorbers which each follow, in offset, a cycle o follow an adsorption phase, at a high pressure of the cycle (Pads), and a regeneration phase ending with a pressurization of the adsorber, and a device for the distillation of purified air 25 comprising an exchange line and a column system, characterized in that it comprises means for storing a liquid containing at least 78% mol of nitrogen, means for vaporizing the liquid containing at least 78% mol.

d'azote et des moyens de raccordement desdits moyens de vaporisation aux adsorbeurs de l'appareil d'épuration, lesquels moyens de raccordement sont 30 adaptés pour pressuriser, au moins partiellement, chaque adsorbeur par l'intermédiaire du liquide vaporisé.  nitrogen and means for connecting said vaporization means to the adsorbers of the purification device, which connection means are adapted to pressurize, at least partially, each adsorber via the vaporized liquid.

Suivant d'autres caractéristiques facultatives de cette installation, l'installation comprend: des moyens pour soutirer un liquide (oxygène, azote ou argon) d'une 35 colonne du système de colonnes, des moyens pour vaporiser ce liquide dans la ligne d'échange et éventuellement des moyens pour pressuriser ce liquide en amont de la ligne d'échange des moyens de stockage d'une partie au moins de l'azote soutiré d'une colonne du système de colonnes.  According to other optional features of this installation, the installation comprises: means for withdrawing a liquid (oxygen, nitrogen or argon) from a column of the column system, means for vaporizing this liquid in the exchange line and possibly means for pressurizing this liquid upstream of the exchange line, means for storing at least part of the nitrogen withdrawn from a column of the column system.

des moyens de stockage d'air liquéfié dans la ligne d'échange.  means for storing liquefied air in the exchange line.

des moyens de surpression d'une partie au moins du liquide contenant au moins 78 % mol d'azote par rapport à la haute pression d'adsorption, les moyens de surpression étant éventuellement agencés en aval des moyens de stockage.  means for overpressuring at least part of the liquid containing at least 78 mol% of nitrogen relative to the high adsorption pressure, the overpressure means possibly being arranged downstream of the storage means.

De préférence, I'appareil de distillation d'air comporte une double colonne, 10 une partie au moins du liquide contenant au moins 78 % mol d'azote étant de l'azote de tête de la colonne moyenne pression et/ ou de la colonne basse pression de la double colonne.  Preferably, the air distillation apparatus comprises a double column, at least part of the liquid containing at least 78 mol% of nitrogen being nitrogen at the head of the medium pressure column and / or of the column. low pressure of the double column.

L'appareil de séparation d'air peut comprendre un seul compresseur qui comprime tout l'air à la pression requise pour vaporiser le liquide pressurisé ou un 15 compresseur qui comprime tout l'air à une pression audessus de la moyenne pression et le surpresseur pour comprimer une partie de l'air à une pression plus élevée. L'invention a également pour objet une installation de distillation d'air, notamment destinée à produire de l'oxygène, du type comportant un appareil 20 d'épuration par adsorption d'air à distiller qui comprend au moins deux adsorbeurs qui suivent chacun, en décalage, un cycle o se succèdent une phase d'adsorption, à une haute pression du cycle (Pads), et une phase de régénération se terminant par une pressurisation de l'adsorbeur, et un appareil de distillation de l'air épuré comprenant une ligne d'échange et un système de colonnes, caractérisée en ce 25 qu'elle comporte des moyens de prélèvement d'un gaz contenant au moins 78 % mol d'azote dans un réseau extérieur et des moyens de raccordement desdits moyens de prélèvement aux adsorbeurs de l'appareil d'épuration, lesquels moyens de raccordement sont adaptés pour pressuriser, au moins partiellement, chaque adsorbeur par l'intermédiaire du gaz.  The air separation apparatus may include a single compressor which compresses all the air to the pressure required to vaporize the pressurized liquid or a compressor which compresses all the air to a pressure above medium pressure and the booster for compress some of the air to a higher pressure. The subject of the invention is also an air distillation installation, in particular intended for producing oxygen, of the type comprising a purification device 20 by adsorption of air to be distilled which comprises at least two adsorbers which each follow, in offset, a cycle o follow an adsorption phase, at a high pressure of the cycle (Pads), and a regeneration phase ending with a pressurization of the adsorber, and an apparatus for the distillation of purified air comprising an exchange line and a column system, characterized in that it includes means for withdrawing a gas containing at least 78 mol% of nitrogen from an external network and means for connecting said withdrawal means to adsorbers of the purification apparatus, which connection means are adapted to pressurize, at least partially, each adsorber via the gas.

L'invention sera mieux comprise à la lecture de la description qui va suivre, donnée uniquement à titre d'exemple et faite en se référant aux dessins annexés, sur lesquels: la figure 1 est une vue schématique d'une installation selon l'invention; la figure 2 est un diagramme du cycle de fonctionnement d'un adsorbeur de 35 l'installation de la figure 1; et la figure 3 est une vue schématique d'une variante de l'installation de la figure 1 la figure 4 est une vue schématique d'une autre variante de l'installation de la figure 1.  The invention will be better understood on reading the description which follows, given solely by way of example and made with reference to the appended drawings, in which: FIG. 1 is a schematic view of an installation according to the invention ; Figure 2 is a diagram of the operating cycle of an adsorber of the installation of Figure 1; and FIG. 3 is a schematic view of a variant of the installation of FIG. 1 FIG. 4 is a schematic view of another variant of the installation of FIG. 1

Sur la figure 1 est représentée une installation 1 de distillation d'air selon l'invention Cette installation est par exemple destinée à produire de l'oxygène gazeux OG, ainsi que de l'oxygène liquide OL.  FIG. 1 shows an installation 1 for air distillation according to the invention. This installation is for example intended to produce gaseous oxygen OG, as well as liquid oxygen OL.

L'installation 1 comprend essentiellement: un compresseur d'air 4, un appareil 6 d'épuration d'air par adsorption, lequel appareil comporte, d'une part, deux adsorbeurs 7 A, 7 B sous forme de deux bouteilles contenant chacune des matériaux adsorbants, par exemple du tamis moléculaire avec éventuellement de l'alumine, capable d'adsorber l'eau et le dioxyde de carbone présents dans l'air, et, d'autre part, des conduites et des vannes de raccordement 15 dont la disposition apparaîtra clairement lors de la description du procédé mis en oeuvre dans l'installation 1 et qui permettent de soumettre successivement chaque adsorbeur 7 A, 7 B au flux d'air à distiller et à un gaz de régénération de l'adsorbant; une turbine d'insufflation 5.  The installation 1 essentially comprises: an air compressor 4, an apparatus 6 for purifying air by adsorption, which apparatus comprises, on the one hand, two adsorbers 7 A, 7 B in the form of two bottles each containing adsorbent materials, for example molecular sieve with possibly alumina, capable of absorbing water and carbon dioxide present in the air, and, on the other hand, pipes and connection valves 15 of which the provision will appear clearly during the description of the process implemented in the installation 1 and which make it possible to successively subject each adsorber 7 A, 7 B to the air flow to be distilled and to a gas for regenerating the adsorbent; an insufflation turbine 5.

une ligne principale d'échange thermique 8; un appareil de distillation d'air sous forme d'une double colonne 10 comportant une colonne moyenne pression 12, une colonne basse pression 14 et un vaporiseur-condenseur 16 couplant ces deux colonnes; et un réservoir 18 de stockage d'oxygène liquide, raccordé à une conduite de production 20.  a main heat exchange line 8; an air distillation apparatus in the form of a double column 10 comprising a medium pressure column 12, a low pressure column 14 and a vaporizer-condenser 16 coupling these two columns; and a tank 18 for storing liquid oxygen, connected to a production line 20.

L'installation 1 comporte en outre un réservoir 22 de stockage d'azote liquide NL sous pression, soutiré en un point de soutirage 24 en tête de la colonne moyenne pression 12 L'azote stocké est ensuite mis sous pression par une pompe 26 La pompe 26 est raccordée à un vaporiseur 30 connu en soi et adapté pour vaporiser l'azote liquide au moyen d'un flux calorigène, tel que de l'eau chaude ou 30 de la vapeur d'eau La vaporiseur 30 est reliée aux adsorbeurs 7 A,7 B à travers une vanne 28.  The installation 1 further comprises a reservoir 22 for storing liquid nitrogen under pressure NL, withdrawn at a withdrawal point 24 at the head of the medium pressure column 12 The stored nitrogen is then pressurized by a pump 26 The pump 26 is connected to a vaporizer 30 known per se and suitable for vaporizing liquid nitrogen by means of a circulating flow, such as hot water or water vapor. The vaporizer 30 is connected to the adsorbers 7 A , 7 B through a valve 28.

Le fonctionnement de l'installation 1 de la figure 1 est le suivant.  The operation of the installation 1 in FIG. 1 is as follows.

L'air à distiller, préalablement comprimé par le compresseur 4, est épuré par l'un des adsorbeurs 7 A, 7 B de l'appareil 6, puis refroidi par la ligne principale d'échange thermique 8 jusqu'au voisinage de son point de rosée pour être introduit en cuve de la colonne moyenne pression 12.  The air to be distilled, previously compressed by the compressor 4, is purified by one of the adsorbers 7 A, 7 B of the device 6, then cooled by the main heat exchange line 8 to the vicinity of its point. dew to be introduced into the tank of the medium pressure column 12.

Le vaporiseur-condenseur 16 vaporise de l'oxygène liquide, par exemple en ayant une pureté de 99, 5 %, de la cuve de la colonne basse pression 14, par condensation d'azote gazeux de tête de la colonne moyenne pression 12.  The vaporizer-condenser 16 vaporizes liquid oxygen, for example having a purity of 99.5%, from the tank of the low pressure column 14, by condensation of nitrogen gas at the head of the medium pressure column 12.

Du " liquide riche " LR (air enrichi en oxygène), prélevé en cuve de la colonne moyenne pression 12, est injecté, après détente, à un niveau intermédiaire de la colonne basse pression 14, tandis que de l'azote liquide NL, sensiblement pur, est prélevé en tête de la colonne moyenne pression 12 pour alimenter le 10 réservoir 22 et la tête de la colonne basse pression 14.  "Rich liquid" LR (oxygen-enriched air), taken from the bottom of the medium pressure column 12, is injected, after expansion, at an intermediate level of the low pressure column 14, while liquid nitrogen NL, substantially pure, is taken from the head of the medium pressure column 12 to supply the reservoir 22 and the head of the low pressure column 14.

De l'azote impur ou " résiduaire " NR, soutiré du sommet de la colonne basse pression 14, est renvoyé à la ligne principale d'échange thermique 8, o il provoque le refroidissement de l'air à distiller.  Impure or "waste" nitrogen NR, withdrawn from the top of the low pressure column 14, is returned to the main heat exchange line 8, where it causes the air to be distilled to cool.

De l'oxygène gazeux OG prélevé en cuve de la colonne basse pression 14 15 est également réchauffé à la traversée de la ligne principale d'échange thermique 8 et distribué par une conduite de production 32.  Gaseous oxygen OG taken from the bottom of the low-pressure column 14 15 is also heated at the crossing of the main heat exchange line 8 and distributed by a production line 32.

De l'oxygène liquide OL est soutiré de la cuve de la colonne basse pression 14 et alimente le réservoir de stockage 18.  Liquid oxygen OL is withdrawn from the tank of the low pressure column 14 and feeds the storage tank 18.

Le fonctionnement de l'installation qui vient d'être décrit peut être mis en 20 oeuvre de façon continue, à l'exception du fonctionnement de l'appareil d'épuration 6, qui suit dans le temps un cycle tel que décrit ci-dessous et illustré par la figure 2.  The operation of the installation which has just been described can be implemented continuously, with the exception of the operation of the purification apparatus 6, which follows in time a cycle as described below. and illustrated in Figure 2.

Cependant il est possible que tous les fluides ne soient pas produits en permanence, selon les besoins du client, le cot de l'électricité etc. Sur la figure 2, o les temps t sont portés en abscisses et les pressions 25 absolues P en ordonnées, les traits orientés par des flèches indiquent les mouvements et destinations des courants gazeux, et, en outre le sens de circulation dans respectivement les adsorbeurs 7 A et 7 B: lorsqu'une flèche est dans le sens des ordonnées croissantes (vers le haut du diagramme), le courant est dit à co-courant dans l'adsorbeur Si la flèche dirigée vers le haut est située au30 dessous du trait indiquant la pression dans l'adsorbeur, le courant pénètre dans l'adsorbeur par l'extrémité d'entrée de cet adsorbeur, si la flèche dirigée vers le haut, est située au-dessus du trait indiquant la pression, le courant sort de l'adsorbeur par l'extrémité de sortie de cet adsorbeur; les extrémités d'entrée et de sortie étant respectivement celles de l'air à épurer et de l'air épuré en phase de 35 production; lorsqu'une flèche est dans le sens des ordonnées décroissantes (vers le bas du diagramme), le courant est dit à contre-courant dans l'adsorbeur Si la flèche dirigée vers le bas est située au-dessous du trait indiquant la pression de I'adsorbeur, le courant sort de l'adsorbeur par l'extrémité d'entrée de cet adsorbeur; si la flèche dirigée vers le bas est située au-dessus du trait indiquant la 5 pression, le courant pénètre dans l'adsorbeur par l'extrémité de sortie de cet adsorbeur, les extrémités d'entrée et de sortie étant toujours celles de l'air à épurer et de l'air épuré en phase de production.  However, it is possible that not all fluids are produced permanently, depending on the customer's needs, the cost of electricity, etc. In FIG. 2, where the times t are plotted on the abscissa and the absolute pressures P on the ordinate, the lines oriented by arrows indicate the movements and destinations of the gas streams, and, moreover, the direction of circulation in the adsorbers 7 respectively A and 7 B: when an arrow is in the direction of increasing ordinates (towards the top of the diagram), the current is said to be co-current in the adsorber If the arrow directed upwards is located below the line indicating the pressure in the adsorber, the current enters the adsorber through the inlet end of this adsorber, if the arrow pointing upwards is located above the line indicating the pressure, the current leaves the adsorber through the outlet end of this adsorber; the inlet and outlet ends being respectively those of the air to be purified and the air purified in the production phase; when an arrow is in the direction of decreasing ordinates (down the diagram), the current is said to be against the current in the adsorber If the arrow directed down is located below the line indicating the pressure of I 'adsorber, the current leaves the adsorber through the inlet end of this adsorber; if the downward pointing arrow is located above the line indicating the pressure, the current enters the adsorber through the outlet end of this adsorber, the inlet and outlet ends always being those of the air to be purified and air purified during the production phase.

Le cycle de la figure 2, dont la période T est, à titre d'exemple, égale à 360 minutes environ pour une pression d'adsorption sensiblement égale à 6 bars, 10 comprend 4 étapes successives I à IV.  The cycle of FIG. 2, the period T of which is, for example, equal to approximately 360 minutes for an adsorption pressure substantially equal to 6 bars, 10 comprises 4 successive stages I to IV.

Ces quatre étapes vont maintenant être décrites successivement pour l'adsorbeur 7 A, étant entendu que l'adsorbeur 7 B suit ces mêmes étapes avec un décalage temporel valant sensiblement T, au moyen de vannes de raccordement ouvertes ou fermées désignées par les mêmes références à venir que celles de 15 I'adsorbeur 7 A, la lettre A étant à remplacer par la lettre B et l'état de chaque vanne (ouverte/fermée) étant à inverser (ferméelouverte).  These four steps will now be described successively for the adsorber 7 A, it being understood that the adsorber 7 B follows these same steps with a time difference substantially equal to T, by means of open or closed connection valves designated by the same references to come only those of the adsorber 7 A, the letter A being to be replaced by the letter B and the state of each valve (open / closed) being to be reversed (closed-open).

TT

Lors de l'étape 1, c'est à dire de t = O à t = 2 I'adsorbeur 7 A est en phase 2 ' d'adsorption sous une pression de fonctionnement haute notée Pads, tandis que l'adsorbeur 7 B est en phase de régénération L'air comprimé par le compresseur 4 20 alimente à co-courant l'adsorbeur 7 A, via une vanne 40 A ouverte La sortie de l'adsorbeur 7 A est reliée à la ligne d'échange 8, via une vanne 42 A ouverte.  During step 1, that is to say from t = 0 to t = 2, the adsorber 7 A is in phase 2 ′ of adsorption under a high operating pressure denoted Pads, while the adsorber 7 B is in the regeneration phase The air compressed by the compressor 4 20 co-flows the adsorber 7 A, via an open valve 40 A The outlet of the adsorber 7 A is connected to the exchange line 8, via a valve 42 A open.

Lors des étapes 11, III et IV, I'adsorbeur 7 A est en phase de régénération, tandis que l'adsorbeur 7 B est en phase d'adsorption Plus précisément, lors de l'étape Il, une vanne 44 A de mise à l'air de l'adsorbeur 7 A est ouverte de façon à 25 ce que la pression à l'intérieur de la bouteille de l'adsorbeur 7 A soit ramenée à une pression sensiblement égale à la pression atmosphérique, notée Patmo sur la figure 2. Lors de l'étape III, la vanne 44 A reste ouverte et de l'azote résiduaire NR soutiré en tête de la colonne basse pression 14 alimente, via une vanne 46 A 30 ouverte, I'adsorbeur 7 A pour y circuler à contre-courant Il s'agit de la phase effective de la régénération pendant laquelle les impuretés sont désorbées et les lits régénérés Lors de l'étape IV, les vannes 44 A et 46 A sont fermées, afin de permettre la pressurisation de l'adsorbeur Dans un premier temps, c'est-à-dire lors d'une première sous-étape IV', la pressurisation de l'adsorbeur est assurée à contre-courant par un flux d'azote gazeux sensiblement pur NG, via une vanne 48 A ouverte, ce flux d'azote gazeux provenant du vaporiseur 30 alimenté en azote liquide par le réservoir 22, via la vanne 28 ouverte Puis, si nécessaire, lors d'une seconde sous-étape IV", la pressurisation est finalisée, également à contrecourant, par prélèvement d'une fraction d'air épurée en sortie de l'adsorbeur 7 B, via une vanne 50 ouverte L'étape IV se poursuit jusqu'à ce que la pression à l'intérieur de l'adsorbeur 7 A soit sensiblement égale à la pression haute Pads.  During steps 11, III and IV, the adsorber 7 A is in the regeneration phase, while the adsorber 7 B is in the adsorption phase More precisely, during step II, a valve 44 A for setting the air of the adsorber 7 A is opened so that the pressure inside the bottle of the adsorber 7 A is reduced to a pressure substantially equal to atmospheric pressure, denoted Patmo in FIG. 2 During stage III, the valve 44 A remains open and residual nitrogen NR withdrawn at the head of the low-pressure column 14 feeds, via a valve 46 A 30, the adsorber 7 A in order to circulate there against -current This is the effective phase of regeneration during which the impurities are desorbed and the beds regenerated. In step IV, the valves 44 A and 46 A are closed, in order to allow the pressurization of the adsorber. a first step, that is to say during a first substep IV ′, the pressurization of the adsorbs ur is provided against the current by a flow of substantially pure nitrogen gas NG, via an open valve 48 A, this flow of nitrogen gas coming from the vaporizer 30 supplied with liquid nitrogen by the reservoir 22, via the valve open 28 Then , if necessary, during a second sub-step IV ", the pressurization is finalized, also against the current, by taking a fraction of purified air at the outlet of the adsorber 7 B, via a valve 50 open L ' step IV continues until the pressure inside the adsorber 7 A is substantially equal to the high pressure Pads.

En conséquence, par le procédé selon l'invention, la pressurisation de 10 chaque adsorbeur ne nécessite plus, pendant la sous-étape IV, d'augmenter le débit du compresseur 4 Avantageusement, l'étape IV ne comporte que la sous étape IV', de sorte qu'aucun débit supplémentaire n'est demandé au compresseur d'air 4 En effet, en choisissant de façon appropriée les conditions opératoires del'installation 1 selon l'invention, il est possible de soutirer continment de l'appareil 15 de distillation d'air suffisamment d'azote liquide, pendant chaque demi-période du cycle de l'appareil d'adsorption, pour assurer l'intégralité de la pressurisation cyclique bouteille d'adsorbant De cette façon, le compresseur 4 est dimensionné de façon optimale, c'est à dire de sorte que son débit nominal soit sensiblement égal au débit d'air traité continment par l'appareil de distillation Les cots 20 d'investissement et de fonctionnement de cet appareil de compression s'en trouvent diminués, par rapport à ceux des installations relevant de l'art antérieur.  Consequently, by the method according to the invention, the pressurization of each adsorber no longer requires, during sub-step IV, to increase the flow rate of the compressor 4 Advantageously, step IV only comprises sub-step IV ' , so that no additional flow is requested from the air compressor 4 Indeed, by appropriately choosing the operating conditions of the installation 1 according to the invention, it is possible to continuously withdraw from the device 15 from distillation of air sufficient liquid nitrogen, during each half-period of the cycle of the adsorption apparatus, to ensure the complete cyclic pressurization of the adsorbent bottle In this way, the compressor 4 is optimally sized , that is to say so that its nominal flow rate is substantially equal to the flow of air continuously processed by the distillation apparatus. The investment and operating costs of this compression apparatus are reduced és, compared to those of installations falling under the prior art.

Le procédé selon l'invention se révèle par ailleurs particulièrement avantageux lorsqu'il est mis en oeuvre au sein d'une installation de distillation d'air disposant préalablement d'un réservoir de stockage d'azote liquide NL, destiné par 25 exemple à être vendu ou exploité par des installations adjacentes distinctes Dans ce cas, il suffit de prélever la fraction d'azote liquide nécessaire au déroulement de la sous- étape IV' précitée.  The method according to the invention also proves to be particularly advantageous when it is implemented within an air distillation installation having beforehand a liquid nitrogen storage tank NL, intended for example to be sold or operated by separate adjacent facilities In this case, it is sufficient to take the fraction of liquid nitrogen necessary for the course of the abovementioned sub-step IV '.

Une partie du gaz de pressurisation contenant au moins 78 % mol d'azote peut provenir d'un conduit général 131 de collecte d'azote gazeux NG sensiblement 30 pur Il est en effet courant que les sites industriels d'implantation d'installations de distillation d'air soient pourvus d'un tel conduit général, I'azote gazeux qui y est véhiculé étant destiné à alimenter diverses installations chimiques ou physicochimiques En présence de ce conduit, il convient de stocker la quantité d'azote gazeux nécessaire à la repressurisation d'un adsorbeur dans le conduit, de façon continue, puis de la prélever cycliquement lors de la repressurisation effective de cet adsorbeur.  Part of the pressurization gas containing at least 78 mol% of nitrogen can come from a general duct 131 for collecting nitrogen gas NG substantially pure 30 It is indeed common for industrial sites setting up distillation installations air are provided with such a general duct, the nitrogen gas which is conveyed therein being intended to supply various chemical or physicochemical installations. In the presence of this duct, it is advisable to store the quantity of nitrogen gas necessary for the repressurization of 'an adsorber in the conduit, continuously, then to take it cyclically during the effective repressurization of this adsorber.

Il est également envisageable que tout le gaz de pressurisation provient du réseau d'azote gazeux.  It is also conceivable that all the pressurization gas comes from the nitrogen gas network.

Si nécessaire, on peut prévoir un compresseur d'azote gazeux pour élever la pression de l'azote gazeux de pressurisation.  If necessary, a nitrogen gas compressor can be provided to raise the pressure of the pressurizing nitrogen gas.

De la même façon, il est possible de réduire les cots d'investissement de l'installation selon l'invention lorsque le procédé selon l'invention est mis en oeuvre dans une installation possédant préalablement une unité de vaporisation, capable 10 d'être aménagée pour permettre la vaporisation d'azote liquide, de la même façon que le vaporiseur dédié 30 décrit ci-dessus Ce vaporiseur peut servir pour produire le gaz de secours.  Likewise, it is possible to reduce the investment costs of the installation according to the invention when the method according to the invention is implemented in an installation having previously a vaporization unit, capable of being fitted out. to allow vaporization of liquid nitrogen, in the same way as the dedicated vaporizer 30 described above. This vaporizer can be used to produce the emergency gas.

Par ailleurs, le fait que l'azote NL produit en continu par la colonne moyenne pression soit sous forme liquide permet de le porter à haute pression moyennant 15 une faible dépense énergétique En particulier, I'azote peut être vaporisé en utiliser la pompe reliée au vaporiseur de secours.  Furthermore, the fact that the nitrogen Nl produced continuously by the medium pressure column is in liquid form makes it possible to bring it to high pressure with a low energy expenditure. In particular, the nitrogen can be vaporized by using the pump connected to the emergency vaporizer.

En effet, pour un même volume final de gaz sous une haute pression, il est énergiquement beaucoup plus coteux de comprimer jusqu'à cette haute pression un volume initial de gaz à basse pression, que de comprimer jusqu'à cette haute 20 pression, puis de vaporiser un volume adéquat de liquide.  Indeed, for the same final volume of gas under high pressure, it is energetically much more expensive to compress up to this high pressure an initial volume of gas at low pressure, than to compress to this high pressure, then spray an adequate volume of liquid.

De plus, il est particulièrement avantageux que la pression de stockage dans le réservoir 22 de l'azote liquide soit supérieure à la pression d'adsorption Pads, permettant ainsi de réduire la durée de repressurisation de l'adsorbeur Par exemple, la pression de stockage d'azote liquide est égale à environ 36 bars, pour 25 une pression d'adsorption Pads d'environ 6 bars.  In addition, it is particularly advantageous for the storage pressure in the reservoir 22 of the liquid nitrogen to be higher than the adsorption pressure Pads, thus making it possible to reduce the repressurization time of the adsorber. For example, the storage pressure liquid nitrogen is approximately 36 bars, for a Pads adsorption pressure of approximately 6 bars.

Sur la figure 3 est représentée une variante de l'installation 1 selon l'invention, analogue à celle de la figure 1 aux différences près qui suivent.  In Figure 3 is shown a variant of the installation 1 according to the invention, similar to that of Figure 1 with the following differences.

L'installation 1 de la figure 3 comporte une ligne d'échange 8 o se vaporise l'azote liquide stocké et pressurisé par échange de chaleur avec de l'air 17 destiné 30 à la distillation.  The installation 1 in FIG. 3 comprises an exchange line 8 o vaporizes the stored nitrogen nitrogen and pressurizes it by heat exchange with air 17 intended for distillation.

Les frigories nécessaires à l'appareil sont fournies par détente d'air dans une turbine Claude 15 Le reste de l'air comprimé se liquéfie et est envoyé à la colonne moyenne pression sous forme du débit 17 Une partie de l'azote pressurisé 19 sert comme produit de l'installation.  The frigories necessary for the device are supplied by air expansion in a Claude turbine 15 The rest of the compressed air liquefies and is sent to the medium pressure column in the form of a flow 17 Part of the pressurized nitrogen 19 serves as a product of the installation.

Toutefois la quantité d'azote requise pour la pressurisation est tellement petite qu'il est possible de la vaporiser dans la ligne d'échange contre un débit d'air à une pression supérieure de quelques bars à la moyenne pression, auquel cas il n'y a aucune liquéfaction de l'air Dans ce cas, tout l'azote vaporisé est envoyé à la pressurisation. Un débit d'oxygène liquide OL est pressurisé par la pompe 50 et se vaporise dans la ligne d'échange 8 pour former le débit gazeux 32.  However, the quantity of nitrogen required for pressurization is so small that it is possible to vaporize it in the exchange line against an air flow at a pressure a few bars higher than the medium pressure, in which case there is no there is no liquefaction of the air In this case, all of the vaporized nitrogen is sent to pressurization. A liquid oxygen flow OL is pressurized by the pump 50 and vaporizes in the exchange line 8 to form the gas flow 32.

Il est également possible de fournir une partie du gaz de pressurisation en soutirant un gaz contenant au moins 78 % mol d'une colonne de l'appareil et en le 10 pressurisant, de sorte qu'il puisse être mélangé avec le gaz de pressurisation résultant de la vaporisation d'un liquide.  It is also possible to supply part of the pressurizing gas by withdrawing a gas containing at least 78 mol% from a column of the apparatus and by pressurizing it, so that it can be mixed with the resulting pressurizing gas. vaporization of a liquid.

Par exemple, on peut envisager, pour la sous-étape IV', d'utiliser en complément au débit comprimé NG un flux de résiduaire NR comprimé au moins à Pads par un compresseur d'azote dédié.  For example, it can be envisaged, for sub-step IV ', to use, in addition to the compressed flow rate NG, a waste stream NR compressed at least at Pads by a dedicated nitrogen compressor.

On comprend que les aménagements respectifs des installations selon l'invention des figures 1 et 3 peuvent être combinés de façon à ce que la repressurisation cyclique de chaque adsorbeur soit assurée à la fois par la vaporisation d'azote liquide NL dans le vaporiseur dédié 30 et dans la ligne d'échange 8 Les installations des Figures 1 et 3 peuvent être modifiées pour 20 prévoir une production d'oxygène gazeux par pompage d'oxygène liquide et vaporisation dans la ligne d'échange 8.  It is understood that the respective arrangements of the installations according to the invention of FIGS. 1 and 3 can be combined so that the cyclic repressurization of each adsorber is ensured both by the vaporization of liquid nitrogen NL in the dedicated vaporizer 30 and in the exchange line 8 The installations in FIGS. 1 and 3 can be modified to provide for the production of gaseous oxygen by pumping liquid oxygen and vaporization in the exchange line 8.

Il est envisageable que le liquide contenant au moins 78 mol % azote soit produit uniquement quand les besoins du client sont réduits et/ou quand le cot de l'électricité est bas afin de constituer une quantité de liquide suffisante pour fournir 25 le gaz de pressurisation pendant tout le fonctionnement de l'appareil de séparation d'air. Selon la Figure 4, le gaz utilisé pour la pressurisation n'est plus de l'azote provenant d'une colonne de l'appareil, mais un débit d'air produit par vaporisation d'un débit d'air sous forme liquide.  It is conceivable that the liquid containing at least 78 mol% nitrogen is produced only when the needs of the customer are reduced and / or when the cost of electricity is low in order to constitute a quantity of liquid sufficient to supply the pressurization gas. during the entire operation of the air separation device. According to Figure 4, the gas used for pressurization is no longer nitrogen from a column of the device, but an air flow produced by vaporization of an air flow in liquid form.

De l'oxygène liquide OL est soutiré de la colonne basse pression et envoyé à la ligne d'échange 8 o il se vaporise Ce liquide peut être pressurisé en amont de la ligne d'échange par une pompe 50.  Liquid oxygen OL is withdrawn from the low pressure column and sent to the exchange line 8 where it vaporizes. This liquid can be pressurized upstream of the exchange line by a pump 50.

L'air gazeux envoyé à la ligne d'échange est divisé en deux, une partie de l'air étant envoyé à une turbine Claude 15 et le reste étant liquéfié dans la ligne 35 d'échange L'air liquéfié est divisé en deux, une partie étant envoyée à la colonne moyenne pression 12 et le reste au stockage 22 A L'air est ensuite vaporisé dans le vaporiseur 30 contre un flux calorigène 3, éventuellement après une étape de pompage. Il sera compris que l'invention s'applique à n'importe lequel appareil de 5 séparation d'air ayant une épuration du type PSA L'appareil peut comprendre une seule colonne, trois colonnes (haute pression, moyenne pression, basse pression), une colonne de mélange ou une colonne argon.  The gaseous air sent to the exchange line is divided into two, part of the air being sent to a Claude 15 turbine and the rest being liquefied in the exchange line. The liquefied air is divided into two, a part being sent to the medium pressure column 12 and the rest to storage 22 A The air is then vaporized in the vaporizer 30 against a circulating flow 3, possibly after a pumping step. It will be understood that the invention applies to any air separation device having a PSA type purification. The device can comprise a single column, three columns (high pressure, medium pressure, low pressure), a mixing column or an argon column.

Un seul stockage de liquide peut alimenter plusieurs appareils de séparation d'air ou être alimenté par plusieurs appareils de séparation d'air.  A single liquid storage can supply several air separation devices or be supplied by several air separation devices.

Les frigories peuvent être fournies par une ou plusieurs turbines de type classique (turbine Claude, turbine d'insufflation, turbine hydraulique, turbine d'azote moyenne ou haute pression) et éventuellement par biberonnage.  The frigories can be supplied by one or more turbines of the conventional type (Claude turbine, insufflation turbine, hydraulic turbine, medium or high pressure nitrogen turbine) and possibly by bottle feeding.

Claims (13)

REVENDICATIONS 1 Procédé de distillation d'air, notamment destiné à produire de I'oxygène, du type dans lequel l'air à distiller est préalablement épuré au moyen d'au moins deux adsorbeurs ( 7 A, 7 B) qui suivent chacun, en décalage, un cycle o se succèdent une phase d'adsorption, à une haute pression du cycle (Pads), et une phase de régénération se terminant par une repressurisation de I'adsorbeur, l'air épuré est refroidi dans une ligne d'échange ( 8) et ensuite envoyé à une colonne de distillation ( 12) d'un système de colonnes et des fluides enrichis en oxygène et en 10 azote sont soutirés d'une colonne ( 14) du système de colonnes caractérisé en ce qu'on utilise un gaz ( 31) contenant au moins 78 % mol d'azote, produit par vaporisation d'un liquide stocké dans un stockage ( 22,22 A) pour pressuriser, au moins partiellement, I'adsorbeur terminant sa phase de régénération.  1 Air distillation process, in particular intended for producing oxygen, of the type in which the air to be distilled is previously purified by means of at least two adsorbers (7 A, 7 B) which each follow, offset , a cycle o follow an adsorption phase, at a high pressure of the cycle (Pads), and a regeneration phase ending with a repressurization of the adsorber, the purified air is cooled in an exchange line ( 8) and then sent to a distillation column (12) of a column system and fluids enriched in oxygen and in nitrogen are withdrawn from a column (14) of the column system characterized in that a gas (31) containing at least 78% mol of nitrogen, produced by vaporization of a liquid stored in a repository (22.22 A) to pressurize, at least partially, the adsorber ending its regeneration phase. 2 Procédé selon la revendication 1, caractérisé en ce que le liquide provient 15 de la ligne d'échange ( 8) ou d'une colonne ( 12,14) du système de colonnes.  2 Method according to claim 1, characterized in that the liquid comes from the exchange line (8) or from a column (12,14) of the column system. 3 Procédé selon la revendication I ou 2, caractérisé en ce que le gaz contenant au moins 78 % moil d'azote utilisé pour pressuriser chaque adsorbeur ( 7 A, 7 B) est à une pression supérieure à la haute pression de la phase d'adsorption (Pabs).  3 Method according to claim I or 2, characterized in that the gas containing at least 78% nitrogen moil used to pressurize each adsorber (7 A, 7 B) is at a pressure higher than the high pressure of the phase of adsorption (Pabs). 4 Procédé selon la revendication 3, caractérisé en ce qu'une partie au moins du gaz contenant au moins 78 % mol d'azote utilisé pour pressuriser chaque adsorbeur ( 7 A, 7 B) est stockée sous une pression de stockage inférieure à la haute pression de la phase d'adsorption (Pads).  4 Method according to claim 3, characterized in that at least part of the gas containing at least 78 mol% of nitrogen used to pressurize each adsorber (7 A, 7 B) is stored under a storage pressure lower than the high pressure of the adsorption phase (Pads). Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en 25 ce qu' une partie au moins du gaz contenant au moins 78 % mol d'azote utilisé pour pressuriser chaque adsorbeur ( 7 A, 7 B) est de l'air et provient de la ligne d'échange ( 8).  Process according to any one of Claims 1 to 4, characterized in that at least part of the gas containing at least 78 mol% of nitrogen used to pressurize each adsorber (7 A, 7 B) is air and comes from the exchange line (8). 6 Procédé selon la revendication 5, caractérisé en ce qu'une partie au moins de l'air utilisé pour pressuriser chaque adsorbeur ( 7 A, 7 B) est stockée sous 30 forme liquide en aval de la ligne d'échange ( 8).  6 Method according to claim 5, characterized in that at least part of the air used to pressurize each adsorber (7 A, 7 B) is stored in liquid form downstream of the exchange line (8). 7 Procédé selon l'une quelconque des revendications 1 à 6, du type à double colonne ( 10), caractérisé en ce que une partie au moins le gaz contenant au moins 78 % mol d'azote utilisé pour pressuriser chaque adsorbeur est de l'azote de tête de la colonne moyenne pression ( 12) et/ ou basse pression ( 14) de la 35 double colonne.  7 Method according to any one of claims 1 to 6, of the double column type (10), characterized in that at least part of the gas containing at least 78 mol% of nitrogen used to pressurize each adsorber is nitrogen at the top of the medium pressure (12) and / or low pressure (14) column of the double column. 8 Procédé selon l'une quelconque des revendications 1 à 7 dans lequel le liquide stocké se vaporise dans la ligne d'échange ( 8) de l'appareil par échange de chaleur avec l'air à distiller ou dans un vaporiseur dédié ( 30).  8 A method according to any one of claims 1 to 7 wherein the stored liquid vaporizes in the exchange line (8) of the device by heat exchange with the air to be distilled or in a dedicated vaporizer (30) . 9 Installation de distillation d'air, notamment destinée à produire de 5 l'oxygène, du type comportant un appareil ( 6) d'épuration par adsorption d'air à distiller qui comprend au moins deux adsorbeurs ( 7 A, 7 B) qui suivent chacun, en décalage, un cycle o se succèdent une phase d'adsorption, à une haute pression du cycle (Pads), et une phase de régénération se terminant par une pressurisation de l'adsorbeur, et un appareil ( 10) de distillation de l'air épuré comprenant une ligne 10 d'échange ( 8) et un système de colonnes ( 12,14), caractérisée en ce qu'elle comporte des moyens ( 22;  9 Air distillation installation, in particular intended for producing oxygen, of the type comprising an apparatus (6) for purification by adsorption of air to be distilled which comprises at least two adsorbers (7 A, 7 B) which each follow, in offset, a cycle in which an adsorption phase follows, at a high pressure of the cycle (Pads), and a regeneration phase ending with a pressurization of the adsorber, and a distillation apparatus (10) purified air comprising an exchange line (8) and a system of columns (12,14), characterized in that it comprises means (22; 22 A) de stockage d'un liquide contenant au moins 78 % mol d'azote, des moyens ( 8,30) de vaporisation du liquide contenant au moins 78 % mol d'azote et des moyens de raccordement desdits moyens de vaporisation aux adsorbeurs ( 7 A, 7 B) de l'appareil d'épuration ( 6), lesquels moyens de 15 raccordement sont adaptés pour pressuriser, au moins partiellement, chaque adsorbeur par l'intermédiaire du liquide vaporisé. 22 A) for storing a liquid containing at least 78% mol of nitrogen, means (8,30) for vaporizing the liquid containing at least 78% mol of nitrogen and means for connecting said vaporization means to the adsorbers (7 A, 7 B) of the purification apparatus (6), which connection means are adapted to pressurize, at least partially, each adsorber via the vaporized liquid. Installation selon la revendication 9, caractérisée en ce qu'elle comprend des moyens ( 22) de stockage d'une partie au moins de l'azote soutiré d'une colonne du système de colonnes.  Installation according to claim 9, characterized in that it comprises means (22) for storing at least part of the nitrogen withdrawn from a column of the column system. 11 Installation selon la revendication 9 ou 10 caractérisée en ce qu'elle comprend des moyens de stockage ( 22 A) d'air liquéfié dans la ligne d'échange.  11 Installation according to claim 9 or 10 characterized in that it comprises storage means (22 A) of liquefied air in the exchange line. 12 Installation selon la revendication 9,10 ou 11, caractérisée en ce qu'elle comporte des moyens ( 26) de surpression d'une partie au moins du liquide contenant au moins 78 % mol d'azote par rapport à la haute pression d'adsorption 25 (Pads).  12 Installation according to claim 9,10 or 11, characterized in that it comprises means (26) for overpressuring at least part of the liquid containing at least 78 mol% of nitrogen relative to the high pressure of adsorption 25 (Pads). 13 Installation selon la revendication 12, caractérisée en ce que les moyens de surpression ( 26) sont agencés en aval des moyens de stockage ( 22; 22 A).  13 Installation according to claim 12, characterized in that the overpressure means (26) are arranged downstream of the storage means (22; 22 A). 14 Installation selon l'une quelconque des revendications 8 à 13, caractérisée en ce que l'appareil de distillation d'air comporte une double colonne 30 ( 10), une partie au moins du liquide contenant au moins 78 % mol d'azote étant de l'azote de tête de la colonne moyenne pression ( 12) et/ ou de la colonne basse pression ( 14) de la double colonne.  14 Installation according to any one of claims 8 to 13, characterized in that the air distillation apparatus comprises a double column 30 (10), at least part of the liquid containing at least 78% mol of nitrogen being nitrogen from the top of the medium pressure column (12) and / or the low pressure column (14) of the double column.
FR0216141A 2002-12-19 2002-12-19 Improved air distillation process, for oxygen production, uses vaporized gas from storage for at least partial pressurization of adsorber ending regeneration phase Withdrawn FR2849172A1 (en)

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FR2910604A1 (en) * 2006-12-22 2008-06-27 Air Liquide Cryogenic distillation apparatus for cold box, has storage container provided with vaporizer for vaporizing liquid, transmitting unit sending calorigenic gas to vaporizer, and dump valve drawing out liquid from storage container
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EP3671086A1 (en) * 2018-12-21 2020-06-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude A method and apparatus for reducing process disturbances during pressurization of an adsorber in an air separation unit
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FR2896860A1 (en) * 2006-01-31 2007-08-03 Air Liquide Air separation method for use in purification installation, involves separating part of purified air in medium pressure column into oxygen and nitrogen enriched liquids, and sending liquid from column to low pressure column
US8713964B2 (en) 2006-12-22 2014-05-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating a gas mixture by cryogenic distillation
FR2910604A1 (en) * 2006-12-22 2008-06-27 Air Liquide Cryogenic distillation apparatus for cold box, has storage container provided with vaporizer for vaporizing liquid, transmitting unit sending calorigenic gas to vaporizer, and dump valve drawing out liquid from storage container
WO2008084167A2 (en) * 2006-12-22 2008-07-17 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating a gas mixture by cryogenic distillation
WO2008084167A3 (en) * 2006-12-22 2009-05-22 Air Liquide Method and device for separating a gas mixture by cryogenic distillation
US9546815B2 (en) 2006-12-22 2017-01-17 L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude Method and device for separating a gas mixture by cryogenic distillation
CN101595356B (en) * 2006-12-22 2012-11-28 乔治洛德方法研究和开发液化空气有限公司 Method and device for separating a gas mixture by cryogenic distillation
CN101441023A (en) * 2007-11-23 2009-05-27 山东科技大学 Energy-saving type air separation process
CN102514701B (en) * 2011-12-07 2014-02-19 中国舰船研究设计中心 System and method for guaranteeing oxygen supply on ship
CN102514701A (en) * 2011-12-07 2012-06-27 中国舰船研究设计中心 System and method for guaranteeing oxygen supply on ship
US10895417B2 (en) 2016-03-25 2021-01-19 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with improved front end purification and air compression
US11619443B2 (en) 2016-03-25 2023-04-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with improved front end purification and air compression
EP3671086A1 (en) * 2018-12-21 2020-06-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude A method and apparatus for reducing process disturbances during pressurization of an adsorber in an air separation unit
US11029086B2 (en) 2018-12-21 2021-06-08 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for reducing process disturbances during pressurization of an adsorber in an air separation unit
US11137205B2 (en) 2018-12-21 2021-10-05 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for eliminating heat bumps following regeneration of adsorbers in an air separation unit
US11612850B2 (en) 2019-11-08 2023-03-28 L'Air Liquide, Societe Anonyme Por L'Etude Et L'Exploitation Des Procedes Georges Claude Pressure equalizing system for air separation purification and control method

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