MXPA98002917A - Process and combustion device in stages for the regeneration of a reformation catalyst or for the production of aromatic compounds in milk mo - Google Patents

Abstract

The invention relates to a regeneration process of a moving bed of reforming catalyst or production of aromatic hydrocarbons, said catalyst includes a support, at least one noble metal and at least one halogen, the process comprises a step of combustion with treatment of the catalyst in at least 2 successive combustion zones, process in which: - each combustion zone is separated from the adjacent combustion zones in order to allow the catalyst to pass through and prevent the passage of gases, - in each zone it is introduced at least one gas containing oxygen and the gases produced are extracted from each zone, - the severity of the operating conditions in each zone increases with the direction of runoff or flow of the catalyst. Advantageously, the combustion stage is terminated in a control zone at the end of the combustion, characterized by a small consumption if not zero oxygen. The invention also relates to the apparatus for putting this process into operation

Description

PROCESS AND COMBUSTION DEVICE KN KTAPA * FOR THE REGENERATION OF A CATALYST OF REFORMATION OR FOR THE PRODUCTION OF CONNECTIONS AROMATICS IN MOBILE BED DESCRIPTION OF THE INVENTION The invention relates to the processes in moving bed for the production of aromatic hydrocarbons, and mainly the reformation. This invention relates more particularly to the combustion stage used at the time of regeneration of the catalyst used and intended to restore their initial catalytic operations.

The catalyst generally comprises a support (for example formed of at least one refractory oxide, the support can also include one or more zeolites), at least one noble metal (preferably platinum), and preferably at least one promoter metal ( for example tin or rhenium), at least one halogen and optionally one or more additional elements (such as alkali metals, alkaline earth metals, lanthanides, silicon, REF: 27283 elements of group IV B, non-noble metals, elements of group III A, etc.,) . Catalysts of this type contain, for example, platinum and at least one other metal deposited on a chlorinated alumina support. In a general manner, these catalysts are used for the conversion of naphthenic or paraffinic hydrocarbons capable of being transformed by dehydrocyclization and / or dehydrogenation; in the reformation or for the production of hydrocarbons, aromatics (for example the production of benzene, toluene, ortho-, meta- or paraxylenes). These hydrocarbons come from the fractionation of crude oils by distillation, or by other transformation processes. These catalysts are widely described in the literature.

One of the means to increase the yields of these processes of reforming or producing aromatic hydrocarbons is to reduce the operating pressures at which the different interesting reactions are carried out. For example, 30 years ago the reformation reactions were carried out at 40 bar; 20 years ago at 15 bar. Nowadays, it is common to see reformers working at pressures below 10 bar, mainly between 3 and 8 bar.

The improvement of the beneficial reactions due to the decrease in pressure is accompanied by a faster deactivation of the catalyst by coking or cocaing. Coke, composed of high molecular weight and consisting essentially of carbon and halogen, is deposited on the active sites of the catalyst. The molar ratio H / C of the formed coke varies from approximately 0.3 to 1.0. The carbon and hydrogen atoms form condensed polyaromatic structures where the degree of crystalline organization is variable depending on the nature of the catalyst and the operating conditions of the reactors. Although the conversion selectivity of the hydrocarbons in coke is very small, the proportions of coke accumulated on the catalyst can be important. Typically, for fixed bed units, these ratios are between 2.0 and 20.0 to 25.51 by weight. For circulating bed units, these proportions are less than 10.0% by weight.

The coke deposit, faster at low pressure, needs an equally quick regeneration of the catalyst. The current regeneration cycles can be reduced to 2 to 3 days.

The European Patent EP-A-0, 378, 482 of the applicant, discloses a continuous regeneration process of a reforming catalyst or production of aromatic hydrocarbons, which allows to alleviate the inherent disadvantages of these more or less short cycles. One of the stages of the regeneration is the combustion of the coke deposited on the catalyst. The present invention relates to this stage.

According to the European Patent EP-A-0,378,482, the catalyst used is progressively moved from the upper part downwards in a regeneration chamber where it successively finds a first zone of mobile and radial bed of combustion, a second zone of moving and radial combustion bed, an axial moving oxychlorination bed zone and an axial moving bed zone of calcination, and (a) in the first combustion zone, the catalyst is treated under a pressure of 3. at 8 bars substantially equal to that prevailing in the first reactor, at a temperature comprised between 350 and 450 ° C by means of a combustion gas based on an inert gas circulating at co-current of the catalyst, which includes 0.01 to 1% of oxygen in volume, this combustion gas coming from a zone of washing gases from calcination, oxychlorination and combustion, (b) in the second combustion zone, the catalyst coming directly from the first combustion zone it is treated under a pressure of 3 to 8 bar, substantially equal to that prevailing in the first reactor, at a temperature higher than at least 20 ° C at the temperature prevailing in the first combustion zone, in the presence of of gases that come from the first combustion zone, and in the presence of a complementary inert gas to which is added up to 20% by volume of oxygen, so that the catalyst is at least in contact with a gas that includes 0.01 to 1 % of oxygen in volume, circulating these gases to co-current of the catalyst.

The catalyst is then sent to the oxychlorination zone.

In order to increase the prior art more clearly, a figure of the European patent EP-A-0 376, 482 showing the catalyst driven by the pipe (17a), stored in the area (20), has been presented in figure 1. and then passes in regeneration through the pipes (9) to a first combustion zone (101), then to a combustion zone - (105). The combustion takes place with an injection (102) of a gas loaded with oxygen (0.01 to 1% by volume) and a supplementary supply (104) of inert gas that can be, if necessary, loaded with oxygen or air. The whole of the combustion stage corresponds to part A of figure 1.

Now, the applicant has been able to verify, after the exploitation of this process, that a good knowledge of the combustion, and therefore of its continuous production and of its control, shows guarantees of a good running of the unit and of a good quality of the regeneration. The applicant has thus sought to improve the control of combustion. The process proposed in the present patent application allows this result to be obtained by the separate management of the gases at the level of each zone, thus controlling the conditions in each combustion zone, and preferably ending the combustion by a control of the end of the combustion.

More specifically, the invention aims at a regeneration process of a moving bed of reforming catalyst or production of aromatic hydrocarbons, said catalyst includes a support, at least one noble metal and at least one halogen, the process comprises a combustion stage with treatment of the catalyst in at least two successive combustion zones, process characterized in that: each combustion zone is separated from the adjacent combustion zones, in order to be able to pass the catalyst and prevent the passage of gases, in each zone introduces at least one gas containing • oxygen and the gases produced are extracted from each zone, the severity of the operating conditions in each zone increases with the flow direction of the catalyst.

Preferably, the gas extracted in a combustion zone is sent at least in part, and preferably in its entirety, to the next zone (in the direction of the catalyst flow) with an optional oxygen supplementation (for example air). ).

In general, to make the operating conditions severe, it is necessary to increase the temperature and / or the oxygen proportion of the incoming gas. Preferably, for each zone the proportion of oxygen in the incoming gas is between 0.01 and 2%, the temperature of the incoming gas is between 350 and 600 ° C, the residence time of the catalyst in a zone is between 5 minutes and 3 hours and the PPH (mass cost per hour of the gas / mass of the catalyst in contact with the gas) is comprised between 1 and 50 h "1.

Advantageously, the combustion stage is terminated by a last so-called control zone for the end of combustion, in which the oxygen consumption is approximately less than 10% of the oxygen entering said zone. The temperature is preferably substantially constant.

Preferably, the control zone is located in the lower part of the last combustion zone, and therefore after the end of the front of the flame.

In addition, a gas containing oxygen in an amount greater than that of the incoming gases is introduced into the control zone at the upstream levels (in the direction of the flow of the catalyst).

Thus, combustion in several zones (or stages) is defined in the present invention, where each stage is characterized by a temperature prevailing in said stage, an inlet temperature of the oxygen-containing gas, an oxygen proportion of the gas entering, an expense or velocity of the gas and a duration of exposure of the coked catalyst to these conditions, in order to have a more efficient combustion.

The description of the invention will be more easily followed with reference to Figure 2, which can be compared with Figure 1 relating to the prior art.

Figures 3 and 4 also show the embodiments of the invention, figure 3 another arrangement of the control area and figure 4 a gas management method.

Figure 2 represents only the combustion stage, or part A of the regeneration process.

In a conventional manner, the catalyst C used to regenerate enters the upper zone or head (2) of the regeneration chamber E through the conduit (1).

The catalyst is then introduced into the conduits or jambs (3) in a first combustion zone Zl. In this zone the catalyst undergoes a first distillation or combustion with the help of a gas containing the oxygen Gl introduced by the conduit (4).

In general, the combustion zones are of the radial type, and preferably annular in the case of the moving bed shown in figure 2, the bed then drains into the annular space delimited by two coaxial cylindrical walls, the gas entering through a wall and leaving by the other.

In the case of the moving catalyst bed, the runoff or flow is continuous. Intermittent flows can also be considered.

The gas G '1 after the passage to this first combustion zone is extracted from said zone by the conduit (5).

The catalyst C descends by the jambs (6) or other conduits to the second combustion zone Z2, into which a gas G2 containing oxygen is introduced through a pipe (7).

According to the invention, the combustion zones Z1 and Z2 are successive and adjacent, that is to say that the catalyst leaving the combustion zone Z1 passes directly to the combustion zone Z2, not undergoing treatment between the two zones. The combustion zones Z1 and Z2 are physically separated so as to allow the passage of the catalyst, but preventing the passage of the gases, for example the passage of the gases G '1 to Z2.

The expert in the field will choose the most adapted means to fulfill this function. In the embodiment of figure 2, a plate (8) for this effect is placed between the zones Zl and Z2 over the entire section of the regeneration chamber E, with the exception of the sections reserved for the passage of the catalyst (jambs u other conduits). Of course, some gas G '1 passes into zone Z2 with the catalyst in the jambs (6), but it is a minimum part of the gas.

The gas G '2 after passing into this second combustion zone is extracted from said zone by the conduit (9); more generally the gas coming from the last zone of the combustion stage is decanted from the enclosure. The catalyst C descends in the jambs or other conduits (10) to the oxychlorination zone, not shown here. This is treated after combustion in a known manner to ensure its regeneration (oxychlorination, calcination). It will also be noted that, preferably, gases coming from the oxychlorination zone are transported from the oxychlorination zone to avoid their passage to the last zone of the combustion stage. In this way, no introduction of chlorine or chlorinated compound into the gases entering into the combustion zones Zl and Z2.

In figure 2 two successive combustion zones have been represented, the number of combustion zones is chosen by the person skilled in the art according to the installation to be conceived. These work and are arranged in the same way as the areas described above.

According to an advantageous embodiment, the gas G '1 leaving the zone Z1 is introduced at least in part, and preferably completely, into the zone Z2 with the gas G2, or after an eventual supplementation of the gas. oxygen to form the gas G2; this arrangement allows a maximum use of the remaining oxygen and a minimum oxygen supply.

This management or separate treatment of the gases at the level of each combustion zone, allows to know precisely at any time the temperatures of the gases entering and leaving, and their amounts of oxygen. In addition to a maximum use of oxygen, this management or treatment allows a domain of combustion of the coke by the control of the operating conditions at the level of each zone.

Preferably, a control operation is carried out at the end of the combustion, in a last zone of the combustion stage.

In the embodiment of Figure 2, this operation is carried out in the lower part (in the direction of flow or runoff of the catalyst) of the last combustion zone Z2, this lower part then constitutes a so-called control zone FC. In the embodiment shown in Figure 3, the control zone FC is a zone not included in the last combustion zone Z2.

The control zone FC is distinguished from a combustion zone since the oxygen consumption is in the FC zone approximately less than 10% of the oxygen entering. Advantageously, the prevailing temperature remains substantially constant (variation of 3% maximum and better than 2% maximum) to the approximate measurement errors and to the approximate thermal waste. In this zone FC a gas G3 containing oxygen enters through the conduit (11) according to figure 2 (and 27 according to figure 3), gas that is extracted after passing through the zone FC, by a duct (9) according to figure 2 by which the evacuation of the gas G '2 that has passed through the combustion zone Z2, or by the duct 28 according to figure 3 is also carried out independently of G'2 .

The person skilled in the art will choose the adapted means for measuring the oxygen consumption in the FC zone. For example, the variation of the oxygen proportion between the input and output of the FC zone can be measured from a variation in the input ratio (equal to the total gas expense) and the measurement of the variation in the proportion at the exit of the zone. In a general way, if the operation of the preceding stages is correct, the oxygen consumption in the FC zone must be small (less than 2-3%).

Another means is to have means for measuring the temperature and / or the proportion of oxygen either on the outgoing gas (for example figure 3 where the gas leaves independently of the other gases coming from the combustion) or on the level of the wall through which the gas exits from the zone FC (case of figure 2 for example).

It is also possible to adapt the means for measuring the temperature of the catalytic bed or of the catalyst entering and leaving the control zone. This mode is provided with a simple means to control the proper functioning of the combustion stages, and by means of the independent management of the gases of each stage, the combustion deficits that vary the temperature can be easily and quickly remedied. or the proportion of oxygen in one or more zones. In fact, if the comparison of the proportions in oxygen or the temperatures on the gases and / or the catalyst leads to variations outside the admissible values for the process (less than 10% for oxygen and at most 3% for temperature) , then at least one operating condition of the at least one combustion zone is modified in order to correct the difference. This can be by modifying the proportion of oxygen and / or the temperature of the incoming gas).

The operating conditions are chosen for each zone and strictly controlled at the level of each zone (contrary to the prior art) in order to reduce as much as possible the harmful effect of combustion on the catalyst. In effect, the products formed by this exothermic reaction are mainly carbon dioxide and water. Now, it is found that these conditions generated by this combustion are undoubtedly the most favorable for aging or for the degradation of the catalyst. In particular, the presence of water at high temperature is responsible for the progressive alteration of the porous support of the catalyst. Typically, the specific surface area of a new catalyst is close to 250 m2 / g. At the end of its life, this value drops to at least 100 m2 / g.

The quality of the combustion is a function of several parameters: the inlet temperature of the gas containing the oxygen, enough to promote the reaction and that accelerates the speed of this reaction, the oxygen proportion of the gas, which has an effect on the rise of the temperature in the bed, and thus on the alteration or not of the catalyst; this also favors the speed of oxygen diffusion in the particle, the amount of oxygen, which determines the amount of coke that can be burned.

In the first phases (or first instants) of the combustion, the oxygen provided is theoretically completely consumed, if the temperature of the gas and the proportion of oxygen are sufficient to trigger the reaction. A part of the coke is very easy and quickly burned at this time.

The applicant has found that coking can be more difficult to burn; At the temperature or the first percentages of coke are easily burned, it takes a very long time to eliminate the other percentages.

This difficulty can, according to the inventors, have several reasons, among others: the presence of different types of coke characterized by firing temperatures or different starts, different crystal organizations, different H / C ratios, location of the coke: coke deposited in the vicinity of the metal phase of the catalyst is more hydrogenated than the coke accumulated on the catalyst support, diffusion problem: the coke on the surface of the catalyst particle burns more easily than that located in the core of the particle . To the problems of chemical reactivity, a problem of diffusion of oxygen is added, towards the coke deposited in the nucleus of the catalyst grain, the size of the coke agglomerations: in thin layer, it is faster to burn than the one that is under the shape of thick agglomerations.

These multiple reasons imply multiple species of coke: cokes at different firing or starting temperatures. Each is characterized by a temperature threshold beyond which the reaction can be triggered satisfactorily and completely. In this case, several operating temperatures can be defined, coke at different burn rates, for example: surface coke and core coke. The first is consumed more quickly in the absence of oxygen. The second is less accessible because it is more "hard" to burn; this constitutes the last percentages of the coke to be eliminated, and can be burned in excess of oxygen if it is considered that there are no more risks of acceleration of the combustion reaction. It is then possible to have a higher proportion of oxygen, and a higher temperature, in order to favor the combustion reaction of this hard coke.

In order to have the conditions on the gas identical, adapted to a "medium" coke as in the prior art, the present invention proposes conditions for the combustion of multiple stages of the coke, carried out in the stages previously described.

Each stage (zone) receives at least one gas containing oxygen at a PPH comprised between 1 and 50 h "1, and preferably 10 to 40 h" 1, and more preferably from 15 to 35 h "1, a temperature T comprised between 350 and 600 ° C, preferably 400 and 600 ° C, an oxygen content (by volume) of at most 2%, and preferably 0.5-1.5%, and generally greater than 0.5%, each zone it has a volume V corresponding to a residence time of the catalyst from 5 minutes to 3 hours.

For each zone, the inlet temperature of the gas containing the oxygen and the proportion of oxygen are such that: the maximum temperature at the outlet of the bed is less than a maximum admissible value, depending on the materials used (for example, 770) ° C for a weakly allied steel). the maximum temperature rise between the inlet and the outlet of the bed is less than 200 ° C, preferably of the order of 100 ° C, - the temperature in the zone is at least 350 ° C, and advantageously at least 400 ° C C, and lower than 600 ° C, preferably lower than 580 ° C and better still at more than 550 ° C. - the temperature in the area is higher than the temperature of the zone immediately preceding it. Thus in zone Z2, temperature T2 is greater than TI of zone Z1.

These more or less elevated temperatures result from the transfer of the hot catalyst from the preceding zone, from the introduction of the hot gas containing the oxygen, and from the exothermic combustion reaction that develops, and from the increasing severity of the operating conditions. .

Preferably, to ensure the proper functioning of the combustion, more or less hot gases are introduced at the level of the zones found at the time of the runoff or flow of the catalyst. In this way, the temperature T2 of the gas G2 will advantageously be greater than that of the gas TI Gl, and T3 will be greater than T2 (T3: temperature of the control zone).

More precisely, in the zone FC a gas enters that has a temperature at least substantially equal to that which prevails at the end of the combustion of the last combustion zone. the oxygen content of the gas introduced is also increasingly greater at the level of the zones found by the catalyst, and the control zone corresponds to the largest proportion of oxygen (amount greater than that of the gas entering the upstream levels). ).

An example of embodiment is schematized in Figure 3, to illustrate the operating conditions of each zone and the management or treatment of the gases.

The regeneration enclosure E is recognized with a mobile bed catalyst C which successively traverses the zones Zl, Z2 and Z3 in which the temperatures TI, T2 and T3 prevail.

The volume of the zones decreases with the direction of runoff or flow of the catalyst. The volumes VI, V2, V3 respectively of the Zl, Z2 and Z3 zones are such that VI > V2 > V3 Different volumes have been chosen in this way, but equal or different volumes are equally considerable in other ways.

A compressor (29) provides a total gas expense divided into three expenditures that feed the zones Zl, Z2 and Z3.

An oxygen analyzer and a temperature meter are placed on each gas flow, in order to eventually adjust the oxygen and temperature ratio to comply with the instructions.

The oxygen supply is made by the pipes 21, 22 and 23 respectively on each gas flow, and the adjustment in the temperature by the means 24, 25, 26 respectively (ovens in Figure 3).

The gases Gl, G2, G3, respectively, whose oxygen content and temperature are in accordance with the setpoint values, enter in this way at the level of each zone Z1, Z2, Z3.

These values of the gases Gl, G2, G3 are, for example, respectively: TI equal to approximately 460 ° C T2 equal to approximately 480 ° C T3 equal to approximately 520 ° C and to the oxygen proportions respectively 01 equal to approximately 0.8 02 equal to approximately 0.8 03 equal to approximately 1.1.

At the level of each zone, a G'l gas results, G'2, G '3 respectively. According to the embodiment of Figure 3, the gases are mixed and collected, at least in part by the compressor (29), in order to reuse them in the combustion, this evidently after at least partial removal of the water and other species from the composition, and after an eventual cooling (by turning off for example) if necessary.

In Figure 3, an arrangement is described in which the gases coming from the combustion and termination zones are mixed, treated and recycled to said zones, as inlet gases.

In a more general manner, the gases extracted at the level of at least 2 zones are collected and reintroduced, after the eventual treatment, at least in part towards at least one combustion zone after an eventual supply of oxygen.

Preferably, there is recycling towards the first combustion zone. The treatment aims to eliminate water and other products of combustion or "parasite" products (such as chlorine).

It is also interesting to foresee that the gas coming from the zone FC (possibly mixed with the gas from the last combustion zone) is reintroduced at least partly towards the zone FC and / or at least partly towards at least one combustion zone. , and preferably the first combustion zone, after evidently of a possible contribution of oxygen to form the inlet gas towards the zone, in order to optimize the oxygen consumption.

In this case, a preferred embodiment for the management or treatment of gases is that shown in Figure 4. The enclosure according to the invention of Figure 2 is recognized with two combustion zones.

Gas G'2 (effluent from the second combustion zone comprising the control zone) is cooled in an exchanger (12), washed in an apparatus (13) to eliminate impurities, mainly chlorinated, and a fraction of this Effluent is purged by the conduit (14), the rest of the effluent is dried in a dryer (16), then compressed in a compressor (15) and separated into two fractions. One is sent as gas Gl to the first combustion zone after reheating (furnace 18) and after the supply of oxygen by a gas (for example air) provided in the conduit (17). The other fraction is reheated (furnace 19), added with oxygen (for example air) - through line (20) and reintroduced as G3 gas in the control zone. The gas G '1 decanted from the first combustion zone is, after the optional supplementation of oxygen through the conduit (20'), introduced into the zone Z2.

It is true that the invention is not limited to this embodiment, it is possible to modify the placement of certain equipment (the dryer after the compressor, for example, preferably especially the effluent) in certain cases reducing the number of equipment (oven 18 for example not used).

The invention also relates to a regeneration chamber that puts this process into operation. Said enclosure includes at least two radial combustion zones (Zl) and (Z2), placed in series, at least one conduit (4, 7) for the introduction of oxygen-containing gas, in each combustion zone, at least one conduit (1) to introduce the catalyst into the enclosure, at least one conduit (3, 6), for the transfer of the catalyst between the zones, and at least one conduit (10) for the transfer of the catalyst to a next oxychlorination zone, and at least one conduit (9) for the evacuation of the gases coming from the combustion, out of the enclosure, said conduit (9) is located before the oxychlorination zone, characterized the enclosure because: between the combustion zones are placed the separation means that allow the passage of the catalyst between the areas in the conduits for this effect, but that prevent the passage of gases between said zones, and at least one conduit (5, 9) is placed at the level of each zone for extract the gas s coming from the passage through said area.

According to a preferred embodiment (Figure 2), the last combustion zone (Z2) includes in its inner part a zone (FC) called control of the end of combustion, provided with at least one conduit (11) for introducing at least one gas containing oxygen and at least one pipe (9) to extract the gases coming from the passage through the combustion zone (Z2) and the control zone (FC).

According to another preferred embodiment (Figure 3), the last combustion zone (Z2) is followed by a so-called control zone (FC), such that a separation means is placed between the two zones allowing the passage of the catalyst, but which prevents the passage of gases, said control zone is provided with a conduit (27) for the introduction of a gas containing oxygen and a conduit (28) for the evacuation of the gas.

Preferably, at least one duct (5) for evacuating the gases from a combustion zone is connected to at least one duct (7) for introducing oxygen-containing gas into a zone that follows it.

Advantageously, the conduit (28, 9) for evacuating the gas coming from the control zone (FC), is connected to the conduit (4) for the introduction of the gas containing oxygen in the first combustion zone (Zl), of way to recycle at least part of the gas coming from the area (FC) to the area (Zl).

To perform the control of the conditions of 'operation in each zone, on the ducts (4, 7) for the introduction into the enclosure, of gas containing oxygen in each zone, at least one duct is provided to realize an oxygen supplement, possibly at least one means for reheating the gas, and a system for measuring the temperature, the proportion of oxygen and the expense, in order to control and adjust the temperature, the proportion of oxygen and the expense according to the operating instructions.

It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Having described the invention as above, property is claimed as contained in the following:

Claims (19)

1. A regeneration process of a moving bed of reforming catalyst or production of aromatic hydrocarbons, the catalyst includes a support, at least one noble metal and at least one halogen, the process comprises a step of combustion with treatment of the catalyst in at least one two successive combustion zones, the process is characterized in that: each combustion zone is separated from the adjacent combustion zones in order to be able to pass the catalyst and prevent the passage of gases, - in each zone at least one gas is introduced that contains oxygen, and the gases produced are extracted from each zone, the severity of the operating conditions in each zone increases with the direction of runoff or flow of the catalyst.

2. The process according to claim 1, characterized in that the gas extracted from a combustion zone is sent at least in part to the next zone (in the direction of runoff or catalyst flow) with an optional oxygen supplementation.

3. The process according to any of claims 1 or 2, characterized in that the gas extracted from a zone is sent in its entirety to the next zone, with a possible supply of oxygen.

4. The process according to any of the preceding claims, characterized in that the severity of the operating conditions is obtained by increasing the temperature and / or the oxygen proportion of the incoming gas.

5. The process according to the preceding claims, characterized in that for each zone the oxygen ratio of the gas entering is between 0.01 and 2%, the temperature of the gas entering is between 350-600 ° C, the residence time of the catalyst in an area is between 5 minutes and 3 hours, and the PPH is comprised between 1-50 hour-1.

6. The process according to any of the preceding claims, characterized in that the combustion stage is completed in a last so-called control zone of the end of the combustion, in which the oxygen consumption is approximately less than 10% of the oxygen entering the combustion. said area.

7. The process according to claim 6, characterized in that the temperature is substantially constant in the control zone.

8. The process according to claim 4, characterized in that the control zone is located in the lower part of the last combustion zone.

9. The process according to any of claims 6 to 8, characterized in that a gas containing oxygen in an amount greater than that of the gas entering the upstream levels (in the direction of runoff or flow) is introduced into the control zone. of the catalyst).

10. The process according to any of claims 6 to 9, characterized in that the gas coming from the control zone is reintroduced at least partly towards the first combustion zone.

11. The process according to any of claims 6 to 10, characterized in that the gas coming from the control zone is reintroduced at least in part in the control zone.

12. The process according to any of the preceding claims, characterized in that the gases extracted at the level of at least 2 zones are collected and reintroduced at least in part in at least one combustion zone after an eventual supply of oxygen.

13. The process according to any of the preceding claims, comprising a step of combustion with treatment of the catalyst in a first combustion zone, and then in a second combustion zone, characterized the process because the zones are separated from -may to leave pass the catalyst and prevent the passage of gases, the second combustion zone includes in its lower part a control zone of the end of combustion, and the effluent extracted from the first combustion zone is sent in its entirety to the second combustion zone after the supply of oxygen, because, the effluent coming from the second combustion zone is cooled, treated to eliminate impurities, purged, dried, compressed and then separated into two fractions, one is introduced after reheating and after the supply of oxygen to the first combustion zone, and the other is reheated, added with oxygen and introduced into the control zone.

14. An enclosure for the regeneration of reforming catalyst or production of aromatic hydrocarbons, including a support, at least one noble metal and at least one halogen, the catalyst is in the form of a moving bed, the enclosure includes at least 2 zones of radial combustion Zl and Z2 placed in series, at least one conduit for the introduction of oxygen-containing gas in each combustion zone, at least one conduit for the introduction of the catalyst into the enclosure, at least one conduit for the transfer of catalyst between the zones and at least one conduit for the transfer of catalyst in a zone following the oxychlorination, and at least one conduit for the evacuation of the gases exiting the combustion towards the outside of the enclosure, this last conduit is located before the zone of oxychlorination, the enclosure is characterized in that: between the combustion zones are located the separation means that allow the passage of the catalyst between the areas in the conduits for that effect, but that prevent the passage of gases between said zones, and at least one conduit is placed at the level of each zone to extract the gases coming from the passage through said zone.

15. The enclosure according to claim 14, characterized in that the last combustion zone Z2 includes in its lower part a so-called control zone FC of the end of combustion, provided with at least one conduit for introducing at least one gas containing oxygen and at least one duct for extracting the gases coming from the passage through the combustion zone Z2 and the control zone FC.

16. The enclosure according to claim 15, characterized in that the last combustion zone Z2 is followed by a control zone FC, such that a separation means is placed between the two zones which allows the passage of the catalyst, but which prevents the passage of the gases, said control zone is provided with a conduit for the introduction of a gas containing oxygen and a conduit for the evacuation of the gas.

17. The enclosure according to any of claims 14 to 16, characterized in that at least one duct for evacuating the gases from a combustion zone is connected to at least one duct for introducing gas containing oxygen, in a second zone that he goes on.

18. The enclosure according to any of claims 14 to 17, characterized in that the gas evacuation conduit coming from the control zone FC is connected to the conduit for the introduction of the oxygen-containing gas, in the first combustion zone Zl of way to recycle at least part of the gas from the FC zone to the Zl zone.

19. The enclosure according to any of claims 14 to 18, characterized in that on the ducts for the introduction into the enclosure, of gases containing oxygen in each zone, at least one duct is provided for making an oxygen supply, and a system for measuring the temperature, the proportion of oxygen and the expense, in order to control and adjust the temperature, the proportion of oxygen and the expense according to the operating instructions. SUMMARY OF THE INVENTION The invention relates to a regeneration process of a moving bed of reforming catalyst or production of aromatic hydrocarbons, said catalyst includes a support, at least one noble metal and at least one halogen, the process comprises a step of combustion with treatment of the catalyst in at least 2 successive combustion zones, a process in which: each combustion zone is separated from the adjacent combustion zones in order to allow the catalyst to pass through and prevent the passage of gases, in each zone it is introduced into the combustion zone. less a gas that contains oxygen and the gases produced are extracted from each zone, the severity of the operating conditions in each zone increases with the direction of runoff or flow of the catalyst. Advantageously, the combustion stage is terminated in a control zone at the end of the combustion, characterized by a small consumption if not zero oxygen. The invention also relates to the apparatus for putting this process into operation.