EP3928044A1

EP3928044A1 - System and method for separating low-pressure gases in the air

Info

Publication number: EP3928044A1
Application number: EP20710578.4A
Authority: EP
Inventors: Benoit Davidian
Original assignee: Air Liquide SA; LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Current assignee: Air Liquide SA; LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date: 2019-02-21
Filing date: 2020-02-12
Publication date: 2021-12-29
Also published as: CN113383203B; US20220065530A1; WO2020169901A1; FR3093008B1; FR3093008A1; CN113383203A; US12098883B2

Abstract

System for separating gases in the air, comprising in the travel direction of the air-stream: - a compression means (1) for compressing the air-stream at a pressure P1 of between 1.15 bar abs and 2 bar abs, - a TSA-type adsorption unit (2), and - a cryogenic distillation unit (3), - with the adsorption unit comprising at least two adsorbers A and B each having a casing having a parallelepiped shape arranged horizontally and comprising: - an inlet and an outlet of the air-stream - a fixed-bed adsorbent mass, also having a parallelepiped shape, the sides of which are parallel to the sides of the casing; and - a set of volumes enabling the adsorbent mass to pass through the air-stream horizontally, over the entire cross-section thereof and over the entire thickness thereof.

Description

Installation and process for separation of gases from air at low pressure

The present invention relates to an installation for separating gases from air and to the process for separating gases from air using this installation. More precisely, it is a question of purifying the atmospheric air before separation of said air by cryogenic distillation.

It is known that atmospheric air contains compounds which must be eliminated before its introduction into the heat exchangers of the cold box of an air separation unit, in particular water vapor (H20), carbon dioxide ( C02), nitrogen oxides and hydrocarbons.

Indeed, in the absence of such treatment of the air to eliminate its impurities H20 and C02, there is a solidification of these impurities during the cooling of the air to cryogenic temperature typically below -150 ° C. , from which it can result problems of clogging of the equipment, in particular the heat exchangers, the distillation columns ...

In addition, it is also customary to at least partially remove the hydrocarbon and nitrogen oxides impurities that may be present in the air in order to avoid their excessive concentration at the bottom of the distillation column (s). , and thus mitigate any risk of equipment degradation.

Currently, this pre-treatment of the air is carried out, depending on the case, by the PSA process (Pressure Swing Adsorption = adsorption at modulated pressure) or by the TSA process (Temperature Swing Adsorption = adsorption with temperature variation). These processes are differentiated by the way in which the regeneration of the adsorbent is carried out: pressure effect in the case where said regeneration takes place thanks to a pressure lower than the adsorption pressure or temperature effect when it takes place at a temperature. temperature higher than that of adsorption. It should be noted that there may also be a pressure reducing effect in a TSA type unit and different designations may be used in this case. In this document, the term “TSA” is used when a temperature effect is used to regenerate, whether or not there is an additional effect linked to the pressure.

Conventionally, a TSA air purification process cycle comprises the following steps: Purification of the air at super-atmospheric pressure and at ambient temperature, optionally of the order of 5 to 10 ° C when using a means of refrigeration upstream of the unit a) Depressurization of the adsorber to atmospheric pressure,

b) Regeneration of the adsorbent at atmospheric pressure, in particular with impure nitrogen coming from the air separation unit and heated to a temperature usually between 90 and 250 ° C by means of an exchanger generally of electric heater or steam heater,

c) Cooling the adsorbent to room temperature, in particular by continuing to introduce said waste gas from the air separation unit but not heated, d) Repressurization of the adsorber with atmospheric air or 'purified air, for example from the adsorber in the production phase.

Generally, the air pre-treatment plants comprise two adsorbers, operating alternately, that is to say that one of the adsorbers is in the production phase while the other is in the regeneration phase.

Additional steps to those described above can be added, such as a step of paralleling the two adsorbers, of varying duration, that is to say from a few seconds to several minutes or else a waiting step. without circulation of fluids through the adsorbent, for example at the end of the regeneration step.

As the pressure facilitates the stopping of impurities, the purification unit is very generally installed after compression, that is to say at a pressure greater than 3 bar abs, frequently at a pressure greater than 4.5 bar abs. This pressure actually depends on the cryogenic cycle selected for the separation of the air.

The cycle most used is the "double column" cycle (conventional dual column cycle) in which the air is compressed to a single pressure which corresponds, except for pressure drops, to the operating pressure of the so-called medium pressure column, that is to say, very generally between 4.5 and 6 bar abs.

There are more complex cryogenic cycles in which air is used both on average (MP, typically 4.5 to 9 bar abs) and high (HP, typically 10 to 65 bar abs, or even 90 bar abs) pressures. The highest pressure is obtained either by compressing again the adequate fraction of the air to medium pressure or by using two compressors (MP, HP) compressing the atmospheric air to the required pressures. It is possible to use two purification units, one in MP for the fraction of the air directly used at this pressure and one in HP for the part compressed at high pressure, to minimize the volume of adsorbent to be put in. artwork. This solution is proposed in document FR 2949846 with the first pressure between 5 and 9 bar abs abs, or even between 2 and 4 bar abs abs. Nevertheless, for the sake of simplicity and generally because of a lower investment, the solution consisting in purifying all the air in PM is usually adopted. An example of this type of cycle is described in document EP 0 789 208 B1, see in particular FIG. 1, with a pressure MP, after first compression, of 5 to 6 bar abs. Fractions of the air thus purified are then overpressed.

It is understood that if the pressure promotes adsorption, it requires in return, greater mechanical strength of the equipment related to purification, in particular of the envelopes of the adsorbers. Several types of adsorbers are used for this air purification application: cylindrical adsorber with vertical axis, cylindrical adsorber with horizontal axis, radial adsorber. It can be noted that all the ferrules used are cylindrical. This is explained by the fact that a cylinder is much more resistant to internal pressure than are flat surfaces.

The energy consumed for the separation of the air being essentially linked to the energy necessary for the compression of the air, the pressure losses must be minimized throughout the circuits having an influence on this pressure in order to obtain a optimal specific energy of separation. Pressure losses through air purification represent a non-negligible part of the irreversibilities of the process. It has therefore been a fundamental trend to develop adsorbers with a minimum brake on the circulation of fluids. The use of the adsorbent in a thin layer and with a large passage section is one of the solutions generally adopted regardless of the type of adsorber, but such a choice has drawbacks.

As shown schematically in Figure 1 [Fig 1], such an arrangement results in large dead volumes on either side of the adsorbent volume. The diagrams la, b and c respectively represent cylindrical adsorbers with a vertical and horizontal axis and a radial adsorber. The adsorbent volumes when used in thin films are only a fraction of the total internal volume of the adsorber, typically less than 50%. This fraction tends to decrease when the size of the adsorbers is increased. Some of these dead volumes are necessary to ensure good distribution of the air and of the regeneration gas through the adsorbent volume. As mentioned at the start of the document, for this application a very thorough purification is sought in the various impurities, in particular for hydrocarbons, especially for propane, and oxides. nitrogen, generally well below one ppm (parts per million). This results in large distribution zones at the inlet and at the outlet of the adsorber in order to have a homogeneous distribution. This also imposes particularly low filling tolerances in order to have adsorbent layers of the same thickness and of the same density (or same void rate) whatever the path of the fluids through the adsorbent, in order to avoid any bypass of air which would pollute the production before the end of the purification stage.

It will be noted that in the case of radial beds, it is possible to obtain, thanks to the implementation of concentric cylindrical grids, bed thicknesses which are practically identical to within manufacturing tolerances. On the other hand, in the case of cylindrical adsorbers with a vertical or horizontal axis, it is necessary to have very flat free surfaces after filling and to ensure that they thus remain in operation. On sections that may exceed 10 m2, this requires adequate installation procedures and / or devices.

If the filling of cylindrical adsorbers can be done relatively efficiently and homogeneously due to their geometry, this is not always the case with radial beds for which it is generally necessary to use equipment developed specially for this purpose and / or provide removable equipment in the upper part.

This translates into a relatively high investment for this medium pressure purification both because of the volume of the envelope, the thickness of the wall and, when good distribution of fluids is required through low beds. thickness, adequate facilities to provide. There have therefore been many developments in an attempt to reduce this cost, in particular proposals to use atmospheric pressure scrubbing units to replace the MP scrub or at least to reduce its size.

In particular, schemes have been developed with total or partial air purification at atmospheric pressure, located at the suction of the air compressor.

Document US 2005/0217481 describes such a system using a technology made possible by low pressure, that of adsorbent wheels (Low Pressure Rotary Adsorbent Contactors). This process is said to be suitable for the purification of air before cryogenic separation. When one seeks to obtain the almost complete stop of the impurities (ultra high purity), it is advisable to use 3 Installations in series.

Always using the technology of adsorbent wheels, it was imagined to put in series, before compression, a rotary system intended to remove the majority of the humidity. followed by conventional purification to remove residual impurities. One can then cite document US 2017/0216760 which, although applied to a VPSA, describes such a dual system.

It should be noted that rotary systems were initially developed to remove part of the humidity from the air at atmospheric pressure in an air conditioning process and not for extensive purification. For these last applications, it is advisable to adapt them by increasing the tightnesses, both between fluids and with the outside and by increasing the stages in series. The industrialization for the envisaged application remains to be carried out for the moment to our knowledge.

These sealing problems of rotary systems are all the more troublesome the further away from atmospheric pressure.

It should be noted here that the drop in the adsorption pressure of MP to atmospheric pressure has a double, if not triple, negative impact. At the same content, the quantity adsorbed is appreciably lower, this is in particular true for CO 2, traces of hydrocarbons and nitrogen oxides. This leads to a first increase in the volume of adsorbent. The quantity of water to be stopped in the atmospheric air is very appreciably greater than that of the air MP. A large part of the water is effectively eliminated in liquid form at the outlet of the final refrigerant of the air compressor in the MP solution. This leads to a consequent increase in the volume of desiccant. But the adsorption of this water also has the effect of heating the air circulating through the adsorbent, again reducing the adsorption capacity of CO 2 and other impurities.

In practice, this means that the solutions consisting in placing the air purification at atmospheric pressure are not completely satisfactory and relatively little used. The potential gains in equipment and technology associated with the use of low pressure are fully offset by the difficulties that low pressure causes in stopping impurities.

Hybrid solutions have therefore also been proposed with partial purification at atmospheric pressure followed by final purification at medium pressure. The final purification is small compared to a conventional solution but the fact of having to implement two units compensates for the gains that could be expected from such a reduction.

Ultimately, there is currently no purification process that can take advantage of low pressure technology and PM purification. A solution of the present invention is an air gas separation installation comprising in the direction of circulation of the air flow:

a compression means 1 making it possible to compress the air flow to a pressure PI of between 1.15 bar abs and 2 bar abs,

a TSA 2 type adsorption unit, and

a cryogenic distillation unit 3,

with the adsorption unit comprising at least two adsorbers A and B each having a parallelepiped shaped envelope arranged horizontally and comprising: an inlet and an outlet for the air flow

an adsorbent mass in a fixed bed also of parallelepiped shape, the faces of which are parallel to the faces of the envelope; and

a set of volumes allowing the flow of air to pass through the adsorbent mass horizontally, over its entire section and over its entire thickness.

The fluids circulate horizontally through the adsorbent mass. The latter can thus be maintained between two walls porous to gases for which the tolerances on the spacing can be very low. It is thus possible to obtain very thin and very homogeneous bed thicknesses. As already indicated, it is practically impossible to achieve this level of precision with a flat adsorbent bed having a large free surface.

In the remainder of the present application, L will denote the length of the adsorber A, H its height and I its width. The section of the adsorbent mass also has a length L and a height H.

The choice of the pressure PI is fundamental in the context of the invention. This pressure must be low enough to allow low-pressure technology for the adsorbers, that is to say in practice adsorber envelopes with flat surfaces and no longer cylindrical envelopes, but also be appreciably higher than atmospheric pressure for limit the negative effects listed above. A pressure of 1.5 bar abs for example makes it possible to use parallelepipedic adsorbers with possibly some reinforcements at the level of the flat surfaces. It also allows a very appreciable gain compared to a solution at atmospheric pressure. The partial pressures of the impurities increase by 50% and, these impurities being in the form of traces, the adsorption capacity of the adsorbents used also increases, as a first approximation by 50%. The The amount of water that can be introduced is smaller and the corresponding temperature rise smaller.

At the same adsorption time, the purification at 1.5 bar abs remains significantly more voluminous than a purification in MP, at 3 or 4 bar abs, but also much more efficient than a purification at atmospheric pressure. The use of low pressure technology for the envelope can then tip the scales in favor of the solution according to the invention.

By fixed beds is meant here that the adsorbent, whether in the form of particles (beads, sticks, granules, platelets, etc.) or of structured adsorbent such as, for example, a monolith, is immobile in an envelope itself. even motionless. This is to exclude any solution where the adsorbent is mobile and in particular any rotary system of the wheel or absillet bar type (process in which it is the envelopes containing the adsorbent which are mobile).

Note that the parallelepipedal shape of the envelope of adsorber A allows dense and homogeneous filling of the adsorber without having to use a complex filling system.

It should also be noted that the crossing of the adsorbent mass by the gas flow horizontally and over its entire length makes it possible to use very thin (0.15 m for example) and very homogeneous adsorbent bed thicknesses.

Depending on the case, the installation according to the invention may have one or more of the characteristics below:

the adsorbers A and B comprise an inlet and an outlet for the regeneration stream; Note that the inlet and outlet of the regeneration flow may be confused with the inlet and outlet of the air flow;

at least one of the adsorbents of the adsorbent mass is in the form of particles;

said installation comprises between the compression means 1 and the cryogenic distillation unit 3 a single adsorption unit.

the set of volumes comprises a first volume VI for introducing and distributing the air flow; a second volume V2 comprising the adsorbent mass; and a third volume V3 for recovering the purified air flow; the three volumes being contiguous and in fluid communication by their common faces; preferably the 3 volumes VI, V 2, and V3 are of parallelepipedal shape and are each of length L, height H and respective widths 11, 12, 13 with 11 <1, 12 <1, 13 <I;

the second volume V2 comprises at least two sub-volumes comprising different adsorbents; these sub-volumes are preferably parallelepipedal in shape and have a height and a length equal to the height and length of the volume V2

the volume VI and / or the volume V3 respectively comprise sub-volume Vll-V12 and V31-V32 separated by a perforated wall improving the distribution of fluids, the volumes VI or VII and V3 or V32 each have at least one side permeable to fluids and the adsorber comprises fluid distribution and recovery boxes contiguous to the permeable faces; these distribution and recovery boxes are preferably in the shape of a half cylinder; they can strengthen the mechanical strength of the adsorber and limit the number of reinforcements that may be necessary; for example, the air flow can be made to enter through a distribution box and the waste gas to exit through a recovery box if this facilitates installation;

the volume V2 or at least one of the sub-volumes of the volume V2 comprises over the entire length of its upper end a system intended to prevent potential local pollution of the purified air; This pollution can be linked to a bypass or a regeneration fault;

the adsorption unit comprises N pairs of adsorbers with N> 1, each pair comprising an adsorber A and an adsorber B placed side by side so as to form a single parallelepiped; preferably, the adsorbers of the same pair are installed symmetrically with respect to their adjacent face. If we look at the parallelepiped formed by the pair of adsorbers, the volumes relating to the introduction of the air to be purified are preferably located on the outside of the parallelepiped and the volumes relating to the introduction of the regeneration gas are preferably located in a central position, each pair of adsorbers comprises an adsorber A in adsorption and an adsorber B in regeneration, with all the adsorption adsorbers operating in parallel and all the regenerating adsorbers operating in parallel,

each adsorber A or B or the pair of adsorbers A / B is installed in an ISO container or in a container with dimensions and gripping installation in accordance with ISO standards; note that preferably at least part of the structure of the container serves directly as a structure for the adsorber (s); preferably also at least part of the equipment annexed to the adsorption such as the valves and the regeneration gas heater is installed in the container;

adsorbers A and B include external or internal thermal insulation on at least part of their faces.

the envelope of adsorber A and / or adsorber B has a length L of between 2 and 15 meters; a height H of between 1 and 3 meters; and a width I of between 0.5 and 3 meters, preferably between 0.8 and 1.2 meters.

The adsorber A of the installation according to the invention will be described in more detail with the aid of FIG. 2. In fact, this figure shows the various volumes V1, V2 and V3 as well as any sub-volumes. The term “parallelepipedal shape” is intended to mean that the casing of the adsorber has in practice its six flat faces and the appearance of a parallelepiped, but that it may include reinforcements, locally at least one layer of insulation. internal or external, and obviously the pipes or boxes for the introduction and withdrawal of air and regeneration gas. The adsorber being laid flat, we call L its great length, I its width and H its height. In the context of the invention, it does not matter whether they are external or internal dimensions.

In FIG. 2, it clearly appears that the volumes and sub-volumes are all of parallelepiped shape and all have the same length L and the same height H. The parallelepipeds which they form differ only by their width.

As indicated previously, the volume V2 can comprise a plurality of sub-volumes with each of said sub-volumes being able to contain a different adsorbent.

From the inlet to the outlet, we can thus use activated alumina, doped activated alumina or silica gel to stop most of the water, a 13X zeolite to stop most of the C02, a zeolite exchanged to stop the nitrogen oxides and certain hydrocarbons ... The configuration adopted here is easier than the usual solutions for the implementation of a multi-layer purification with a well-determined geometric volume for each of the beds. The widths I2i can be of different dimensions. This configuration preferably corresponds to the use of particulate adsorbent (ball, rod, etc.). One could also use monoliths or more generally structured adsorbents, with or without the need to have separate sub-volumes. Indeed, depending on the form geometric structure of structured adsorbents, there is no need to systematically provide a separation between elements of different nature which can be arranged directly in series.

[Fig 2] Figure 2 shows a case corresponding to 2 under volume V21 and V22.

According to another embodiment, the volume VI and / or the volume V3 respectively comprise sub-volume V11-V12 and V31-V32 separated by a perforated wall improving the distribution of fluids. By this embodiment, we want to ensure good distribution of the air through the entire section of the adsorbent and similarly, that of the regeneration gas. The perforated part between the volumes Vil and V12 on the one hand and / or between the volumes V31 and V32 on the other hand makes it possible, with a low pressure drop, to significantly improve the distribution of the fluids entering and / or leaving the layers of 'adsorbent. The fluidic resistance of the adsorbent layers themselves then makes it possible to obtain very quickly, after one or two centimeters, the almost perfect distribution of the flow rates (at + or - 1% if necessary).

In order to guarantee the thermal efficiency of the adsorption unit, that is to say to limit its losses, a preferred embodiment will correspond to the following characteristic:

at least some faces of an adsorber or of a pair of adsorbers have thermal insulation outside or inside the adsorber.

This thermal insulation can use any of the conventional insulating materials (perlite, rock wool, expanded foam, etc.) but also devices such as an air gap or preferably a double air gap system as conventionally used in adsorbers. upstream of cryogenic air separation units. In this case, it is the fluid itself which acts as an insulator.

According to another embodiment, the adsorber A or the pair of adsorbers A - B is installed in an ISO container or in a container with dimensions and gripping installation in accordance with ISO standards.

The adsorber or the two adsorbers are assembled in a specific structure produced in the workshop, which may optionally use part of a standard ISO container. The advantage of complying with ISO standards is that it allows for greatly facilitated handling and transport. Any reinforcements allowing the mechanical resistance of the assembly to pressure will be contained in the standard dimensions of the containers. Given that there are large containers, it may be advantageous, in the two cases above, to also house the distribution boxes, part of the pipes or valves, the electric heater, etc. in the container. At least one of the walls of the container (side, bottom, top wall) can serve as a wall for the adsorber itself. In particular, the side walls can be integrated into the distribution volumes VI and / or V3. More generally, at least part of the structure of the container serves directly as a structure for the adsorber.

The materials used for the adsorbers and their internals are, for example, carbon steel, stainless steel, aluminum, or materials with low thermal expansion, using INVAR.

The present invention also relates to a process for separating gases from air from an air flow containing at least one impurity chosen from water vapor, carbon dioxide, nitrogen oxides and hydrocarbons, using an installation as defined above and comprising the following successive steps: compression 1 of the air flow to a pressure PI between 1.15 bar abs and 2 bar abs, purification of the compressed air flow, by adsorption using the TSA 2 type unit so as to eliminate at least one impurity contained in the air flow, and separation of the constituents of the air flow by cryogenic distillation using the unit (3), with all of step b) carried out at pressure PI.

Depending on the case, the method according to the invention may exhibit one or more of the characteristics below:

the pressure PI is between 1.15 bar abs and 1.5 bar abs, preferably between 1.20 bar abs and 1.30 bar abs.

the method implements an installation as defined above and in step b) the air flow is introduced into the volume VI or the sub-volume Vil and the purified air flow is withdrawn from the volume V3 or the sub -volume V32. It should be noted that this introduction and / or this withdrawal will preferably be carried out either horizontally via one or both lateral sides of the casing, or vertically via one or both horizontal faces of the casing, in other words via the top or the bottom of the envelope, or via a large face of the envelope;

the installation used includes in its adsorption unit N pairs of adsorbers A and B with N> 1 with the adsorbers of the same pair side by side with so as to form a single parallelepiped and with each pair of adsorbers comprising an adsorber A in adsorption and an adsorber B in regeneration, the process comprises an additional step d) of regeneration of the adsorber B and in step b) in each adsorber A in adsorption the air flow is introduced into each volume VI or sub-volume Vil and the purified air flow is withdrawn from each volume V3 or sub-volume V32 and in step d) in each adsorber B in regeneration a regeneration stream is introduced into each volume V3 or sub-volume V32 and then withdrawn from each volume VI or sub-volume Vil.

the air or regeneration flows are introduced or withdrawn from the various volumes VI, Vil, V3 and V32, preferably by their sides located in the side faces of the parallelepipedal shape of the adsorber A or B or by their sides located in the bases of the parallelepipedal shape of the adsorber A or B. In fact, the flows can be introduced / withdrawn theoretically by at least one of the 5 faces of the different volumes facing the external environment (the 2 side faces, the top face or bottom, or possibly the main face LxH). Preferably the side faces or by the base. The main face does not promote distribution and the interior face is not available if 2 adsorbers are placed side by side. As the adsorber is filled from the top, obstacles in the upper part will be avoided.

The method according to the invention is illustrated by Figure 3 [Fig 3]. The atmospheric air 10 containing the various pollutants to be eliminated is compressed by means of the compressor 1 to the pressure PI, of the order of 1.5 bar abs, and this compressed air 11 is introduced into the adsorber A of the TSA. At the purification outlet, this purified air 12 is sent to the downstream part of the unit 3 which comprises in particular the cryogenic distillation unit. Regeneration gas 14 comes from this latter unit. It is generally impure nitrogen (that is to say containing argon and oxygen) at low pressure, close to atmospheric pressure. This gas - or a fraction of this gas - is heated using one or more heat exchangers (steam, electric, heat recovery from other fluids, etc.) during the heating step and then serves to cool the adsorber. The production 13, generally of impure oxygen (90-98%) in the case which interests us, is directed to a downstream unit not shown.

Regarding the entry and withdrawal of fluids, one or more of the following characteristics can be found: • the fluids are introduced or withdrawn from volume VI - or depending on the case of sub volume Vil - horizontally via one or both lateral sides.

• the fluids are introduced or withdrawn from volume V3 -or depending on the case of sub-volume V32- horizontally via one or both lateral sides.

• The fluids are introduced or withdrawn from the volume VI -or depending on the case of the sub-volume Vil- vertically via one or both horizontal faces constituting the top or the bottom of the parallelepiped.

• the fluids are introduced or withdrawn from volume V3 -or depending on the case of sub-volume V32- vertically via one or both horizontal faces constituting the top or bottom of the parallelepiped.

According to another variant, the fluids are introduced or withdrawn via the large faces of the parallelepiped (of section L * H). In the latter case, the circulation of fluids through the adsorber (VI, V2, V3) takes place essentially in a straight line from the inlet to the outlet. This is meant to mean that in particular, there is no sudden change in direction, at approximately 90 °, of the fluid between its entry into the adsorber and its horizontal crossing of the adsorbent volume.

The circulation of fluids being horizontal in the adsorbers, there are some of the constraints specific to radial adsorbers, and in particular the fact that it is necessary to prevent the premature penetration of impurities in the upper part of the adsorber. Said breakthrough may come from a bypass or from an overflow of local air and / or from a regeneration fault.

The bypass can for its part have its origin in the settling of the adsorbent. These problems are well known to those skilled in the art and solutions already developed will be applied here. In particular, as indicated above, the use of parallelepipedal adsorber simplifies, by virtue of its geometry, the implementation of the solutions devised for the radial beds (dead zone filled with a sufficient height of adsorbent, equivalent of cones. .). It should be noted again that the filling is also simplified and that it is easy here to obtain a filling with rain, dense and homogeneous, limiting both the settling and the risks of density inhomogeneity in the beds.

Owing to the simple geometry, it is possible for example to use a balloon inflated to a pressure greater than PI, forming a seal above the free surface of the adsorbents. It could also be a membrane permanently applied to the surface. free from adsorbents by a slight overpressure compared to the operating pressure. This overpressure can come from a fluid, for example instrument air, or from a heavy material. Here again, it will be necessary to adapt the solutions developed for the radial adsorbers of units for the production of oxygen by adsorption.

The following example will illustrate the invention as it has just been described.

It relates to an oxygen production unit of the order of 100 t / d (tonnes / day) for which the air flow rate used is 15,000 Nm3 / h. The pressure PI on leaving the first compression stage is 1.3 bar abs. This air is cooled to 3 ° C by means of a refrigeration unit to limit the quantity of water vapor entrained towards the purification and to lower the adsorption temperature. This temperature is here in the lower range of the temperature levels used. It was chosen mainly because of the low value of PI. Temperatures of 5 to 8 ° C could be adopted, in particular in the event of a slightly higher PI pressure. The final choice stems from a global economic study. The adsorption time used is 150 minutes, resulting in a cycle time of 5 hours given that the purification unit usually comprises 2 adsorbers, one being in production while the other is regenerating. These conventional times could be reduced here. The cryogenic process adopted results in having a large flow of waste gas that can be used for regeneration, which could potentially shorten the usual heating and cooling times. Furthermore, the depressurization and repressurization steps are practically unnecessary given the respective production pressures (1.3 bar abs) and regeneration (1.03 bar abs). However, the low thickness of the activated alumina and zeolite beds, of the order of 0.25 m, did not lead to further possible optimization. Production times of 120, 90, or even 60 minutes can be envisaged with air to be purified, optionally introduced at a temperature above the 3 ° C. used in this example. Taking into account the energy importance of the pressure drops at low pressure, it may be envisaged to install a regulation of the regeneration flow rate based on an optimization of the pressure drop throughout said step. In other words, more flow is taken when the adsorber is relatively cold, for example at the start of heating and at the end of cooling, and less, when, conversely, it is, on average, the hottest. It is also easier to impose a first heating flow rate and a second larger flow rate during cooling. The total volume of adsorbent is of the order of 6 m3 distributed almost half between activated alumina and type X zeolite exchanged with calcium and bar absyum, a particularly efficient adsorbent for stopping traces of hydrocarbons and oxides of nitrogen.

According to the invention, each adsorber is in the form of a parallelepiped of length L equal to 5.75 m, of height H equal to 2.9 m, and of width I equal to 1.00 m.

The useful height of adsorbent is 2.1 m. An anti-pollution system is provided in the upper part, a reserve of adsorbent to compensate for the compaction and 10 pipes for filling the volumes V21 and V22 respectively with activated alumina and with zeolite. Fluids in and out are from the sides. These are boxes, themselves parallelepipedic, joined on either side of the adsorber proper.

The input and output volumes VI and V3 are not here divided into sub-volumes. The widths available for each of them (0.25 m) allow direct introduction, the speed of the fluids being sufficiently low.

The two adsorbers are disposed adjacent with a thermal insulating absrière bar between the facing surfaces. This absrière bar can be constituted simply by an air gap. A variant would consist in keeping only one common wall separating the two adsorbers and in using, on both sides, an internal insulation. This type of insulation is favored by the fact that the fluids circulating in contact with the insulation are dry (purified air, regeneration nitrogen). The adsorbers are made symmetrically so that the volumes V3A of the first adsorber and V3B of the second adsorber are adjacent (apart from the insulation absrière bar, if this solution is retained) in the central part.

This description will be explained with the aid of [Fig 4] and [Fig 5] representing respectively a cross section and a longitudinal section of the two adsorbers as they are installed.

In the Figure [Fig 4], there is therefore shown the two adsorbers A and B. The various references correspond to their outer envelope. They are separated by a barrier 2 ′ providing thermal insulation. This barrier makes it possible to limit the heat losses of the regeneration flow and the heating of the purified air. Depending on the pressure PI and the dimensions of the adsorber, it may include mechanical reinforcements in order to increase the rigidity of the large faces (L * H) of the adsorbers. As we have described, there are several other variations to achieve this isolation. The marks 3 ′ correspond to the volumes VIA and V1B intended for the supply of air to be purified and for the outlet of the regeneration gas. Likewise, the marks 4 'at the outlet of the purified air and at the inlet of the regeneration gas. The volumes V21A and V21B 5 'contain the activated alumina, the volumes V22A and V22B 6' the exchanged zeolite. The walls (7 ', 8', 9 ') are permeable to gases but impermeable to the particles of adsorbent. These are grids or perforated sheets covered with a wire mesh smaller than the minimum particle diameter. He can also choose grids specially developed for this type of application of the “wedge wire screen” type, also commonly called Johnson grid after the name of a supplier. The marks 10 ', 1, 12' and 13 'correspond to the system intended to compensate for the settling of the adsorbent and to prevent a local bypass of impurities. A rectangular metal sheet 10 'extending from one end of the adsorber to the other defines a guard volume 1 filled with adsorbent. The angle of the sheet with the horizontal allows the particles passing through the free space 13 'to completely fill the volume located below this sheet. The adsorbers are filled through the pipes 12 'which have a sealing flange at their upper end.

Figure 5 [Fig 5] is a longitudinal section of adsorbers A and B, adsorber B being an adsorber A in regeneration. It makes it possible to follow the progress of the different fluids. It is assumed that the adsorber A is in the production phase. The air to be purified 20 'enters by the box 14' fixed to one end of the adsorber A. This air is distributed, in part because of the deflector effect due to the lateral outer wall of the adsorber, in the VIA volume. From there, it successively passes through the outer permeable wall, the activated alumina bed 5 ', the middle permeable wall, the zeolite bed 6' and the inner permeable wall. The purified air 2 is collected in the volume V3A then enters the box 15 'before leaving the system. The other adsorber B is then in the regeneration phase. The regeneration gas 30 'enters through the box 15' of this adsorber, follows the reverse path of the air and leaves via the box 14 '. The choice has been made here to allow the hot regeneration gas to enter through the center of the device formed by the two adsorbers. This configuration is not compulsory and, taking into account the inevitable thermal expansions, another arrangement could be retained. A single pipe has been shown for the inlet and outlet of the fluids in the adsorber. Depending on the layout, it may be more judicious to provide two separate pipes, one for the air, the other for the regeneration fluid.

Note that these diagrams have not shown the filter at the outlet of adsorbers. Usually for this type of application, it will be integrated into the adsorbers. Remember that this is possible because, taking into account the circulation of fluids between adsorption and regeneration, these filters are self-cleaning, that is to say that they are automatically unclogged at each cycle. Preferably, the filter is placed in the box 15 '. It is preferably flat.

One of the advantages of using low pressure technology for the construction of adsorbers is to benefit from easy transport between the workshop and the installation site. This possibility nevertheless imposes some dimensional constraints. Thus, an adsorber will preferably have the following characteristics:

a length L between 2 and 15 meters, a height H between 1 and 3 meters and a width I between 0.5 and 3 meters, preferably between 0.8 and 1.5 meters.

It is appropriate a priori to limit the width of the adsorber and more particularly the thickness of the adsorbent layers so that the pressure drops through said adsorbents remain very low, of the order of a few millibars, possibly of around ten. millibars.

This implies that we can effectively join the two adsorbers without the width at all exceeding about 3 m.

These constraints that one wishes to respect on the maximum dimensions of an adsorber mean that the flow of air purified by the TSA unit which has just been described is limited, probably around 30 to 50,000 Nm3 / h according to the exact conditions used for the purification. To go further, we will therefore have to install several identical units in parallel.

As indicated above, this adsorption unit is located upstream of a cryogenic distillation unit. This unit can in particular be well suited to the production of oxygen at low pressure, and in particular to oxygen between 90 and 98% purity.

The installation according to the invention also makes it possible to produce units of small size, that is to say from a few tens to a few hundreds of tonnes per day of oxygen in a competitive manner. The compression means 1 could then be common to several units of possibly different nature (air boosted for combustion, for ventilation, etc.).

Claims

1. Air gas separation installation comprising in the direction of air flow:

- a compression means (1) making it possible to compress the air flow to a pressure PI of between 1.15 bar abs and 2 bar abs,

- a TSA type adsorption unit (2), and

- a cryogenic distillation unit (3),

with the adsorption unit comprising at least two adsorbers A and B each having a parallelepiped shaped casing arranged horizontally and comprising:

- an air flow inlet and outlet

- An adsorbent mass in a fixed bed also of parallelepiped shape, the faces of which are parallel to the faces of the envelope; and

- a set of volumes allowing the passage of the adsorbent mass by the air flow horizontally, over its entire section and over its entire thickness.

2. Installation according to claim 1, characterized in that said installation

comprises between the compression means (1) and the cryogenic distillation unit (3) a single adsorption unit.

3. Air separation installation according to one of claims 1 or 2,

characterized in that the set of volumes comprises:

a first volume VI for introducing and distributing the air flow; a second volume V2 comprising the adsorbent mass; and

a third volume V3 for recovering the purified air flow;

the three volumes being contiguous and in fluid communication by their common faces.

4. Air separation installation according to claim 3, characterized in that the second volume V2 comprises at least two sub-volumes comprising different adsorbents.

5. Air separation installation according to one of claims 3 or 4, characterized in that the volume VI and / or the volume V3 comprise

respectively sub-volume V11-V12 and V31-V32 separated by a perforated wall improving the distribution of fluids.

6. Air separation installation according to one of claims 3 to 5,

characterized in that the volumes VI or Vil and V3 or V32 each have at least one face permeable to fluids and the adsorber comprises fluid distribution and recovery boxes contiguous to the permeable faces.

7. Air separation installation according to one of claims 1 to 6,

characterized in that the adsorption unit comprises N pairs of adsorbers with N> 1, each pair comprising an adsorber A and an adsorber B joined together so as to form a single parallelepiped.

8. Air gas separation installation according to claim 7, characterized in that each pair of adsorbers comprises an adsorber A in adsorption and an adsorber B in regeneration, with all the adsorption adsorbers operating in parallel and all of the adsorbers. Regenerating adsorbers operating in parallel.

9. Air gas separation installation according to one of claims 7 or 8,

characterized in that each adsorber A or B or the pair of adsorbers A / B is installed in an ISO container or in a container with dimensions and gripping installation in accordance with ISO standards.

10. Installation for separating gases from the air according to one of claims 7 to 9,

characterized in that the adsorbers A and B comprise external or internal thermal insulation on at least part of their faces.

11. Air gas separation installation according to one of claims 7 to 10,

characterized in that the envelope of adsorber A and / or adsorber B has: a length L of between 2 and 15 meters;

a height H of between 1 and 3 meters; and

a width I of between 0.5 and 3 meters, preferably between 0.8 and 1.2 meters.

12. A method of separating gases from air from an air flow containing at least one impurity chosen from water vapor, carbon dioxide, nitrogen oxides and hydrocarbons, using an installation as defined in one of claims 1 to 10 and comprising the following successive steps:

a) compression (1) of the air flow to a pressure PI between 1.15 bar abs and 2 bar abs,

b) purification of the compressed air stream, by adsorption using the TSA type unit (2) so as to remove at least one impurity contained in the air stream, and c) separation of the constituents of the air stream. air by cryogenic distillation using unit (3),

with all of step b) carried out at pressure PI.

13. A process for separating gases from air according to claim 12, characterized in that the pressure PI is between 1.15 bar abs and 1.5 bar abs, preferably between 1.20 bar abs and 1, 30 bar abs.

14. A process for separating gases from air according to one of claims 12 or 13,

characterized in that it implements an installation as defined in one of claims 3 to 5 and in step b) the air flow is introduced into the volume VI or the sub-volume Vil and the flow purified air is withdrawn from volume V3 or from sub-volume V32.

15. A process for separating gases from air according to claim 14, characterized in that:

- the installation implemented includes in its adsorption unit N pairs

adsorbers A and B with N> 1 with the adsorbers of the same pair side by side with so as to form a single parallelepiped and with each pair of adsorbers comprising an adsorber A in adsorption and an adsorber B in regeneration,

- the method comprises an additional step d) of regeneration of the adsorber B and

- in step b) in each adsorber A in adsorption, the air flow is introduced into each volume VI or sub-volume Vil and the purified air flow is withdrawn from each volume V3 or sub-volume V32 and at l step d) in each regenerating adsorber B, a regeneration stream is introduced into each volume V3 or sub-volume V32 and then withdrawn from each volume VI or sub-volume V1.

16. Method according to one of claims 14 or 15, characterized in that the air or regeneration flows are introduced or withdrawn from the different volumes VI, Vil, V3 and V32, preferably by their sides located in the side faces of the parallelepipedal shape of the adsorber A or B or by their sides located in the bases of the parallelepipedal shape of the adsorber A or B.