JPS6039110B2 - Continuous conversion method for hydrocarbons - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION This invention relates to the conversion of hydrocarbons, and more particularly to hydrocarbon hydroreforming processes.

The invention also applies to saturated or unsaturated gasolines, such as pyrolysis gasolines, especially steam cracked gasolines,
Aromatic hydrocarbons such as benzene, toluene and xylenes (ortho, meta or para) starting from naphthenic hydrocarbons which can be converted to aromatic hydrocarbons by dehydrogenation It also concerns how to do so. In this method, at least one reactor or reaction zone, preferably several reactors or reaction zones, for example three to four, are used to carry out the reforming reaction or aromatic hydrocarbon production. The reactor includes a fluidized bed of catalyst.

The charge is sequentially circulated through each reactor or reaction zone according to a directional or radial flow (ie, from the center to the periphery or from the periphery to the center).

The reaction zones are arranged in series such that the charge flows sequentially through each of the reaction zones, being heated intermediately between each reaction zone. The new catalyst is placed in the upper part of the reaction zone which receives the new charge. The catalyst then flows progressively from the top to the bottom of this reaction zone and is removed from the lower part by any suitable method (especially lift).
The catalyst is then conveyed to the top of the next reaction zone, through which it also flows progressively from top to bottom, and so on until the last reaction zone, at the bottom of which it is also gradually removed and then into the regeneration zone. send. Below, a unit diagram shows an arrangement of this type with three successive contact strip castles, which is described, for example, in French patent no. 21602
69.

It is desirable to arrange the reaction belts side by side. The removal of catalyst from each reaction zone is also difficult, and by adopting appropriate degrees of intensities and ratios, the level of action and selectivity of the reaction zones can be maintained constant at all times.

Removal of catalyst from each reaction zone Now, as shown above,
Do it gradually.

The term "gradually" means that the catalyst can be removed as follows. That is, 'a} A portion at a time, e.g. 0.5 to more than 15% of the total amount of catalyst, is removed, but periodically, e.g. every 1/10 to 10 days.

However, it is also possible to remove the catalyst with a higher frequency (eg, minutes or seconds) and proportionally less amount. {b) Continuously.

This is currently the preferred method. The circulation of the catalyst from the lower part of one reaction zone to the upper part of the other reaction zone, from the lower part of the last reaction zone to the regeneration zone, and from the regeneration zone to the upper part of the first reaction zone is , with any known lifting and unloading device, which is designated by the word "lift" later in the description and in the claims.

The lift fluid used to deliver the catalyst can be any gas, such as nitrogen, or hydrogen, especially purified hydrogen, or even recycled hydrogen. The solids transferred from the reaction zone to the reaction zone and towards the regeneration zone may be, for example, particulate catalysts with a suitable support.

The catalyst may, for example, be spherical, generally with a diameter in the range of 1 to 3 willows, preferably 1.5 to 2 willows. However, these numerical values are not limited.
The specific gravity of the catalyst in bulk is between 0.4 and 1.
, preferably 0.5 to 0.9, especially 0.6 to 0.8
It is included between. However, these numbers are not limited. The reactions to which the process according to the invention is preferably applied are listed at the beginning of this patent application and can clearly be divided into two groups:

That is, [1} One of them is the 1'' homing reaction.

The general conditions for the catalytic hydroreforming reaction are as follows. That is, the average temperature in each reaction zone is in the range of about 480 to 600 degrees Celsius, or 530 to 60,000 degrees Celsius, the pressure is in the range of about 5 to 20 kg', and the rate of liquid naphtha per one catalyst is 0.5 kg. It ranges from 5 to 1 shipboard, and the recirculation rate ranges from 1 to 10 moles of hydrogen per mole of charge. Specific examples of reforming reactions include the following.

That is, the charge: naphtha distilled in the range of about 6,000 to about 22,000, especially straight naphtha.

Catalyst: The catalyst comprises at least one metal of the platinum group, in other words one of the noble metals such as platinum, palladium, iridium-ruthenium, osmium, supported on a support of alumina or an equivalent compound (e.g. : platinum-alumina-halogen, or platinum-iridium-alumina halogen).

The content of noble metal is 0.1 to 2% by weight based on the catalyst.
The content of halogen, preferably chlorine or fluorine, is 0.
1 to 10%. The alumina halogen bond can be replaced by other supports, such as silica alumina. The catalyst may also include at least one metal promoter selected from across each group on the periodic table of elements. ■
The other one is the production reaction of aromatic hydrocarbons from saturated or unsaturated gasoline.

If the bag contents are unsaturated, in other words contain diolefins and monoolefins, they must first be removed by selective or total hydrogenation.

Then, if the charge contains olefins, the charge from which all of the olefins and a significant amount of the monoolefins have been removed by hydrogenation is then subjected to at least one olefin in each reaction zone. in the presence of a catalyst comprising at least one metal co-catalyst selected from the periodic table of the elements, for example one noble metal of the No. Under a pressure in the range of 60 k9/h, the volumetric flow rate of the liquid charge per hour is about 0.1 to 10 times the volume of the catalyst, and the hydrogen/hydrocarbon (molar ratio) is about 0.5 to 20. Treated with hydrogen. The catalyst used here is a bifunctional catalyst.

That is, it includes an acid function (carrier) and a dehydrogenation function. Acid functions include alumina and alumina containing chlorine and/or fluorine, or silica alumina, silica magnesia,
The dehydrogenation function is caused by acidic compounds such as silica tria and alumina magnesia.
Molybdenum sulfide is like molybdenum.
It is produced by one or more appropriately selected metals held by an acidic carrier. The content by weight of dehydrogenation metals in the catalyst is generally from 0.01 to 5%, preferably 0.05%.
It ranges from 1% to 1%, preferably about 0.10 to 0.6%.

The catalyst may also contain up to about 10% halogen by weight. Regeneration of the catalyst in the strict sense can be carried out using all known methods.

Preference is given to {a) burning the catalyst with the help of a gas containing molecular oxygen; {b} a gas containing molecular oxygen and at the same time a halogen; alternatively, e.g. Oxychlorination using an alkyl compound (c-) Final treatment with the help of a gas containing molecular oxygen.

Regeneration involves purging, for example with nitrogen, to remove all traces of residual oxygen gas from the catalyst.

Generally, before the regenerated catalyst reaches the first reaction zone,
In order to reduce, in other words to reduce certain oxides, especially metal oxides, present in the catalyst, it is treated with hydrogen, which is carried out at between about 450 and 560 CO. In the prior art, when operating in a fluidized bed reaction zone, the reduction is carried out in the upper part of the reactor, i.e. in the very interior of the reactor, and the catalyst is present in its original state in the form of a dense fluidized bed. It descends through the first reaction zone located above the reaction zone, ie, the first reaction zone where reduction takes place.

Heating of the reduction zone is ensured by heating the reactor itself, in particular by indirect contact with the hot charge to be treated. Once the reduction is complete, the catalyst reaches the actual reaction zone, still in the form of a fluidized bed. Similarly, regenerated catalysts are generally
It is desirable that the catalyst undergoes sulfidation during the course of the process, such that all metals contained in the catalyst are clearly sulfided before reaching the actual reaction zone.

The sulfurization reaction takes place either at the head of the reactor, i.e. in the same reaction zone as that in which the reduction takes place, or in a zone just below the reduction zone and in which the catalyst also flows in the form of a fluidized bed. . In sulfide belts, conventional techniques operate at temperatures at which reduction takes place, ie in the range of 500 to 600 degrees Celsius. Moreover, in the reduction zone sulfide zone, in order for the catalyst to have a temperature close to that for the IJ homing reaction or the aromatic hydrocarbon production reaction, it is necessary to
It is necessary to operate in the range 0 to 600°C. The sulfiding agent used is pure hydrogen sulfide or hydrogen sulfide diluted with hydrocarbon gas, or dimethyl disulfide diluted with hydrogen, or other sulfur compounds such as alkyl sulfides, alkylmercabutanes diluted with hydrogen. This is what I did.

The pressure used is that prevailing within the IJ homing or aromatic hydrocarbon production reactor itself, and the duration of the sulfidation reaction varies from a few minutes to several orders of magnitude, depending on the operating conditions selected. The fluidized catalyst bed thus passes through the sulfide zone and then into the reaction zone where the reforming reaction or aromatic hydrocarbon production reaction takes place. carrying out a reduction reaction and sulfidation reaction in the upper part of the first reaction zone;
Prior art methods exhibit various significant drawbacks.

First of all, each reaction zone exhibits extremely large thermal inertia, so there is no way to rapidly vary the temperature in the upper part of the first reaction zone, for example.

This therefore makes it impossible to precisely control either the reduction temperature or the sulfidation temperature, and thus these temperatures are practically equal to the temperature at which the reforming reaction or the aromatic hydrocarbon formation reaction takes place. Become. [b' It follows then that the sulfidation temperature is therefore always the temperature at which reduction takes place, ie 50,000.

Therefore, in order for this sulfurization to be more effective, that is, for sulfur to be more firmly fixed on the metal of the catalyst, it is desirable that the sulfurization temperature is 400° C. or lower. By the way, the ideal sulfiding temperature is 300 to 400oo, even better 320 to 37,000, preferably 310 to 380.
It would be qo. A minimum temperature of 500 qo is therefore prohibitive. {c} Furthermore, the reduction temperature is actually determined by the temperature of the reactor itself.

By the way, in the reaction equipment, the IJ homing reaction or aromatic hydrocarbon production reaction is currently underway at 520 pm.
In addition to the above, since it is held at a temperature of 530 pm or higher,
The reduction temperature is actually preferably in the range of 480 to 530°C or 480 to 520°C, but it is still 52,000°C (or 530qC) or higher. 'd} Finally, in the conventional technology system, the safety conditions are still not sufficient. In fact, the purging of the catalyst with nitrogen following the regeneration of the catalyst makes it possible in principle to remove all the oxygen gas that has become active during the course of the regeneration, thus avoiding the risk of explosion in the reaction zone. However, if this explosion were to occur suddenly due to unspecified causes such as high pressure or accidental leakage, it would quickly spread to the sulfide zone and the reaction zone of reforming and aromatic hydrocarbon production. This is because the reduction reaction and sulfurization reaction zones are located at the head of the first reactor and are close to each other. The method according to the invention overcomes these disadvantages. In this method, the reduction zone and the sulfidation zone are on the one hand separated from each other and, on the other hand, located outside the first reactor. Next, embodiments of the present invention will be described based on the drawings.

In addition, in FIG. 1 and FIG. 2, three reactors are each used. Example 1 In FIG. 1, the charge is first led through conduit 1, furnace 2, channels 3 and 4 to a first reactor 29.

Effluent from the first reactor 29 is removed via conduit 301 and passed through the furnace 37 and conduit 38 to the second reactor 4.
Sent to 2. The effluent from the second reactor 42 is transferred to the conduit 4
3 and sent through a furnace 50 and a conduit 51 to a third reactor 55. Effluent from the third reactor 55 is removed by conduit 56. Fresh catalyst is introduced into the first reactor 29 by a conduit not shown in FIG. 1 upon start-up of the unit. The regenerated catalyst enters the first reactor 29 via a conduit or lift 19 as well as a plurality of conduits 27,28. The catalyst passes through the conduits 27, 28 on the one hand and in the first reactor 9 on the other hand.
It progresses as a fluidized bed. The catalyst is transported from the first reactor 9 to the lift pot 3 along a plurality of conduits 31 and 32.
It is taken out by a conduit 3 which leads to 4.

This removal may be done periodically by any suitable gating system, or, even better, continuously without gating. The regulation of the catalyst flow rate is then ensured by classical means with the help of pure hydrogen or hydrogen produced by the unit, which is injected at the level of the lift pot 34 by a conduit not shown. The gas flow rate of the unit is adjusted to prevent a portion of the reaction effluent from being carried away with the catalyst particles.

The catalyst is then conveyed from the lift pot 34 towards the second reactor 42 by any known tinning device, herein referred to by the term "lift." The fluid in lift 36 may be recycled hydrogen from conduit 35 or hydrogen produced by the unit. The catalyst thus conveyed to the lift 36 reaches a receiver 39 from where it is transferred via a plurality of conduits 40, 41 to a second reactor 4.
Reach 2.

Here, the receiver 39 and the conduits 40, 41 may optionally form part of a second reaction device 42. The catalyst passes through the second reactor 42 as a fluidized bed and, as for the first reactor 29, by a plurality of conduits 44, 45.
It is removed from the second reactor 42 and reaches a lift pot 47 via conduit 46. For example, by means of a lift 49 fed with recycle hydrogen or unit hydrogen coming through conduit 48, the catalyst reaches a receiver 52 and from there via a plurality of conduits 53, 54 to a third reactor 55 of the fluidized bed. reach The catalyst is supplied to the first and second reactors 29, 4.
2, it is removed from the third reactor 55 by a plurality of conduits 57, 58. This spent catalyst reaches lift pot 60' via conduit 9. Then,
This spent catalyst is sent to an "accumulator decanter" flask 7, for example by means of a lift 6 which is fed with recycled hydrogen which is fed by a conduit 61 into a lift pot 60. The spent catalyst passes through a gate valve system 8 and conduit 9 to a regeneration zone 10'. After catalyst regeneration is complete and the regenerated catalyst is purged to remove molecular oxygen (the various feed conduits required for regeneration and purging are conventional and are not shown): This regenerated catalyst is used in the flow paths 11, 13 and the gate valve system 12.
and send it to the receiving flask 15. Therein, the regenerated catalyst is optionally swept away by a stream of pure hydrogen fed through conduit 14 in order to maintain a mildly elevated pressure in receiving flask 15 and against lift pot 17 . The catalyst removed from the flask 15 by conduit 16 thus reaches the lift pot 17 from where it is transported to the first reactor 2 by means of pure hydrogen fed by conduit 18.
Lift 19 towards Kangen Obi Castle 20 located at the top of 9
carried to. If the pure hydrogen in the lift 19 is not sufficient to undertake the reduction, the reduction zone 20 may, as necessary,
It receives a supply of hydrogen sent through a conduit 21. The reduction zone 20 is heated via conduit 5 and conduit 22 by indirect contact with a portion of the bag contents. This divided portion of the charge, after being used to heat the reduction zone 20 in this manner, is then generally then transferred to the two reactors 42.
Alternatively, it is sent directly to either one of 55. This heat is also generated by diverting in a similar manner at least a portion of the effluent from the third reactor 55 coming out of the flow path 56. The portion of the charge or effluent thus diverted towards conduit 5 amounts to 1 to 5% by weight of the total amount of initial charge in conduit 1 or the total amount of initial effluent in conduit 56. It's fine if you have one.

The catalyst flows through the reduction zone 20 as a fluidized bed. The catalyst is then removed from the reduction zone 20 by a plurality of conduits 27, 28, among which also
The catalyst flows as a fluidized bed. The sulfurization of the catalyst with the aid of sulfur compounds and, in some cases, pure hydrogen used as a carrier gas takes place in a conduit or leg 27.
, 28. This combined gas conduit 24, 2
5 and 26 into conduits 27,28. In the conduits or legs 27, 28, the gas turbulence is very strong, thus ensuring a smooth sulfurization reaction. conduit 27
, 28 generally include catalyst, combined gas and conduits 18,
19, 21, it may be necessary to vent the excess pure hydrogen via the withdrawal conduit 23. The regenerated catalyst then enters the first reactor 29 through conduits 27 and 28, reduced and sulphided. Embodiment 2 In FIG. 2, the regeneration belt castle is placed above the reduction belt castle and the sulfidation belt castle.

This layered arrangement is particularly preferred when the reactor is of moderate size. In the figure, the charge is led to a first reactor 29 through a conduit 1, a furnace 2, and channels 3, 4.

Effluent from the first reactor 29 is removed via conduit 30' and passed through a furnace 37 and conduit 38 to the second reactor 4.
Effluent from 2 is removed by conduit 43 and sent through furnace 50 and conduit 51 to a third reactor 55. Effluent from the third reactor 55 is removed by conduit 56. Fresh catalyst is introduced into the first reactor 29 by a conduit, not shown, upon start-up of the unit. Regenerated catalyst enters the first reactor 29 via a plurality of conduits 27,28. The catalyst is on the one hand in conduit 2
7, 28 and on the other hand the first reactor 29
They move through each as a fluidized bed.

The catalyst is removed from the first reactor 29 by a plurality of conduits 31 , 32 and a conduit 33 which brings the catalyst to a lift pot 34 .

This removal can be done periodically by any suitable gating system or, even better, continuously without gating. The regulation of the catalyst flow rate is then ensured by pure hydrogen injected through conduits not shown in FIG. 2 or by classical means by borrowing the hydrogen power generated by the unit. The gas flow rate of the unit is adjusted to prevent a portion of the reaction effluent from being carried away with the catalyst particles.

The catalyst is then conveyed from the lift pot 34 towards the second reactor 42 by any known lifting device, herein referred to by the term "lift." The fluid in lift pot 36 may be recycled hydrogen from conduit 35 or hydrogen produced by the unit. The catalyst thus conveyed to the lift 36 reaches a receiver 39 and from there via a plurality of conduits 40, 41 to a second reactor 42. Here, the receiver 39 and the conduit 4
0,41 may form part of the second reactor 42 in some cases. The catalyst passes through the second reactor 42 as a fluidized bed and is removed from the second reactor 42 by a plurality of conduits 44, 45, as for the first reactor 29, and reaches a lift pot 47 by conduit 46. . For example, by means of a lift 49 fed with recycle hydrogen or unit hydrogen coming through conduit 48, the catalyst reaches a receiver 52 and from there via a plurality of conduits 53, 54 to a third reactor 55 of the fluidized bed. reach The catalyst is
As for the first and second reactors 29, 42, they are removed from the third reactor 55 by a plurality of conduits 57, 58. This spent catalyst reaches lift pot 60' by conduit 59. This spent catalyst is then used in an "accumulator" placed above the first reactor 29, for example for use in a lift 6 fed with recycled hydrogen which is fed by a conduit 61 into a lift pot 60.
Decanter" and send to flask 7. The spent catalyst passes through the gate valve system 8 and conduit 9 to the regeneration belt 10'. After catalyst regeneration is complete and the regenerated catalyst is purged to remove intramolecular oxygen (the various feed conduits required for regeneration and purging are conventional and are not shown): This regenerated catalyst is passed through channels 11, 13 and gate valve system 12 to receiving flask 15. Therein, the regenerated catalyst is optionally swept away by a stream of pure hydrogen fed through the conduit 14 in order to maintain a mildly high pressure in the flask 15 across the reduction zone. Optionally, the receiving flask 15 can also be placed directly at the head of the reducing belt 20.

The catalyst thus removed from flask 15 by conduit 16 and optionally by gate valve system 17 and conduit 18 reaches a reduction zone 20 located below regeneration zone 10 and above first reactor 29 .
The two rivers in the reduction zone receive a supply of pure hydrogen sent through the conduit 21. In the reduction zone 2, either by indirect contact with a portion of the charge via conduits 5, 22 or by conduit 5.
Heated by a portion of the effluent from 6. The catalyst flows through the reduction zone 20 as a fluidized bed. The catalyst is then removed from the reduction zone 20 by a plurality of conduits 27, 28, in which the soot also flows as a fluidized bed. It is in the conduits or legs 27, 28 that the sulfurization of the catalyst takes place with the aid of sulfur compounds and, if necessary, pure hydrogen used as carrier gas. This sulfur compound is led by conduits 24, 25 and 26 to conduits 27, 28. conduit or leg 27,2
8, the gas turbulence is extremely strong, thus ensuring a smooth sulfurization reaction. Conduits 27, 28 generally include:
Since it is full of catalyst, sulfur compounds and pure hydrogen,
It may be necessary to vent excess pure hydrogen via the withdrawal conduit 23. The regenerated catalyst is reduced and sulphided and then enters the first reactor 29 via conduits 27 and 28. The method according to the invention thus exhibits various advantages that the methods of the prior art did not have.

The heating method of the reduction zone 20 and the sulfurization zone conduits 27 and 28 in FIGS. 1 and 2 is completely unrelated to the heating method of the first reactor 29. In these two belts, thermal inertia no longer exists and, for example, with the help of a partial flow of the charge (conduit 5 in FIGS. 1 and 2), the reduction temperature can be adjusted.
With the aid of conduit 24 and conduits 27, 28 of FIGS. 1 and 2, the sulfiding temperature can be easily adjusted to the desired value. In particular, the reduction temperature is generally 480 to 520q.
The temperature can be adjusted to an optimum temperature between 480 and 530 o. Similarly, in prior art methods, it was not possible to reduce the temperature of the sulfide belt since it was contained between two hot belts.

On the other hand, in the present invention, in order to lower the temperature, it is sufficient to appropriately make the conduits 27, 28 where the sulfidation reaction is occurring heat conductive.
Since it disappears at high temperature,
Sulfurization at 300 to 400°C, preferably 310 to 38°C
000°C, for example 320 to 370°C. It is also possible to utilize the temperature of conduit 24 to help control the sulfiding temperature.

In addition, in this method, even if traces of oxygen remain in the regenerated catalyst despite the removal of oxygen and cause an explosion in the reduction zone, this explosion will occur in the reduction zone 20. Spreading to the reactor 29 itself, which is sufficiently separated from the reactor, is unlikely.

Similarly, if necessary, it is easy to cut off the heating in the reduction zone 20 or the sulphidation zone conduits 27, 28, since these two zones are connected to the first reactor 29. This is not possible when the iron is attached to the head.

[Brief explanation of the drawing]

Both FIG. 1 and FIG. 2 are pipe system diagrams showing embodiments of the present invention. Figure 2 Figure 1

Claims (1)

[Claims] 1. A process for the continuous conversion of hydrocarbons in the presence of a catalyst, in which an initial charge of hydrocarbons and hydrogen is circulated through at least one fluidized bed reaction zone, the catalyst comprising: A method in which the catalyst gradually flows from the upper part to the lower part of the reaction zone and circulates through the reaction zone as a fluidized bed, and then the catalyst is gradually taken out from the lower part of the reaction zone and sent to a regeneration zone.
) The regenerated catalyst is sent to a reduction zone in which the reaction zone is separate and is supplied with hydrogen and heated by said charge or a portion of the reaction effluent, said reduction zone having a
operating at a temperature in the range of 0 to 530°C; and (b) the regenerated and reduced catalyst is passed to the reduction zone through a plurality of conduits forming a sulfidation zone that is distinct from the reduction zone and the reaction zone. in a conduit in which the regenerated and reduced catalyst is circulated as a fluidized bed, and in which conduit the regenerated and reduced catalyst is converted into a gas containing sulfur compounds. Thus, a process characterized in that the sulfurization is carried out at a temperature in the range from 300 to 400° C. below the reduction temperature as well as the reaction temperature. 2. The method according to claim 1, wherein the temperature of the reaction zone is in the range of 480 to 600° C. and hydroreforming of hydrocarbons is carried out. 3. The method of claim 2, wherein the temperature is in the range of 530 to 600°C. 4. The method according to claim 1, wherein the temperature of the reaction zone is in the range of 530 to 600°C, and aromatic hydrocarbons are produced. 5. The method according to claim 1, wherein the sulfiding temperature is in the range of 310 to 380°C. 6. The method of claim 1, wherein the portion of the charge or reaction effluent used to heat the reduction zone is about 1 to 5% by weight of the total initial charge or reaction effluent. . 7. The method according to claim 1, wherein the sulfur compound is hydrogen sulfide or dimethyl disulfide. 8. The method of claim 1, wherein the sulfur compound is conveyed by a stream of pure hydrogen. 9. A method according to any one of claims 1 to 8, wherein the catalyst is continuously removed from the reaction zone towards the regeneration zone. 10. A process according to any one of claims 2 to 8, characterized in that at least two reaction zones arranged in succession and arranged in an apparently vertical side-by-side, through which each is of the fluidized bed type,
circulating the charge, the charge is circulated sequentially through each reaction zone, the catalyst is also circulated sequentially through each reaction zone, flowing progressively from the top to the bottom of each reaction zone as a fluidized bed; In a method in which the catalyst is gradually removed from the bottom of the last reaction zone through which the charge has passed and sent to the regeneration zone, the regenerated catalyst is
Before being sent back to the reaction zone, (a) this regenerated catalyst is
a reduction zone which is supplied with pure hydrogen and is separated from a first reaction zone heated by said charge or a portion of the reaction effluent, and whose temperature is in the range of 480 to 530°C. (b)
) The regenerated and reduced catalyst is directed from the reduction zone to the upper part of the first reaction zone through which the charge has passed, through a plurality of conduits forming a sulfidation zone that is separate from the reduction zone and the reaction zone. The regenerated and reduced catalyst is circulated as a fluidized bed in the conduit, and the regenerated and reduced catalyst is heated at the reduction temperature and the reaction temperature by the gas containing the sulfur compound. Below, 300 to 4
A process characterized in that it undergoes sulfidation at a temperature in the range of 00°C. 11. The method of claim 10, wherein the catalyst is removed from each reaction zone sequentially. 12. The method according to claim 10, wherein the temperature of the first reaction zone is in the range of 530 to 600° C. and hydroreforming of hydrocarbons is carried out. 13. The method according to claim 10, wherein the temperature of the first reaction zone is in the range of 530 to 600°C, and the aromatic hydrocarbon is produced. 14. As a re-ascension method that allows the catalyst removed from the regeneration zone to be conducted sequentially to the reduction zone and then to the sulfidation zone, a regeneration zone is placed alongside the reaction zone and said reduction zone and sulfidation zone are themselves regenerated. 14. A process according to any one of claims 1 to 13, located above the reaction zone in which the reduced and then sulphurized catalyst is introduced. 15. A regeneration zone is located above a reduction zone and a sulfidation zone, which are themselves located above a reaction zone in which the regenerated, reduced and then sulfided catalyst is placed. The method according to any one of items 1 to 13.