JPS5911337B2 - Moving bed reactor - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an improvement in a vertical reactor capable of continuously treating, for example, a gaseous or vaporous fluid to be treated over a long period of time. A multi-stage reaction zone loaded with movable solid particles having an activity suitable for the treatment of a fluid, such as a solid catalyst or an adsorbent, the solid particles being loaded into the reaction zone. The present invention relates to a novel vertical mobile reactor that can be replaced during operation of treating the fluid to be treated.

Among the generally known reactors, the one that is particularly frequently used is the fixed bed reactor. Depending on the selection of solid particles, the active life of some particles may not be very long, so if such solid particles must be loaded into the reactor and used, the shape of the reactor should be enlarged. It became necessary to either increase the amount of solid particles charged as much as possible, or to stop the operation shortly after the start of operation and replace the solid particles with new ones.

It should be noted that the necessity of replacing solid particles, which is extremely troublesome, not long after the start of operation, is not limited to cases where solid particles with a short active life as described above are loaded, but also when the particles are highly active. Even when solid particles with a long life are loaded, there are cases where operation is difficult.

This is a case where the activity of the solid particles mentioned above is temporarily deactivated due to incorrect operation. In cases where the gas is manufactured and distributed as city gas, stopping the operation and replacing the catalyst as described above would be a serious social problem, so measures should be taken to prevent this. It was necessary.

Normally, two reactors of the same type are kept on hand for such cases, and while one reactor is being used to treat the fluid to be treated, new solid particles or If regenerated solid particles are loaded in one reactor and the activity of the solid particles loaded in one reactor is deactivated, the flow direction of the fluid to be treated can be changed to the other reactor. A method has been proposed in which the processing operation is continued by switching to .

However, such a method of always having two reactors on hand not only considerably increases the manufacturing cost of the apparatus, including the cost of incidental equipment such as valves and lines for switching the flow direction of the fluid to be treated, but also It has the disadvantage that operation switching operations and the like are very complicated.

On the other hand, as seen in Japanese Patent Application Laid-Open No. 47-42-481, etc., the internal structure of one reactor was improved, instead of having two reactors as mentioned above, and the A method has been proposed in which solid particles that are deactivated during a fluid processing operation are successively replaced with new ones.

However, the moving bed reactor seen in JP-A-47-42481 etc. has a multi-stage annular reaction zone in a reaction vessel having upper and lower solid particle supply ports and solid particle discharge ports, respectively. The device has a structure in which the fluid to be treated sequentially passes through the zone in the radial direction.
For example, if we try to apply such a device (radial flow type reactor) to the steam reforming reaction for producing city gas as mentioned above, it is necessary to increase the diameter of the device or increase the number of stages in the reaction zone. It cannot be said that it is a very good idea because

This is because when trying to produce methane-containing city gas by steam reforming feedstock hydrocarbons in the presence of a nickel-based catalyst, for example, when the feedstock hydrocarbons are reformed in the catalyst layer near the feedstock hydrocarbon inlet, A decomposition reaction (endothermic reaction) occurs, followed by a methane production reaction (exothermic reaction) to obtain the final product gas. This is because unreacted gas will flow out of the system unless the catalyst layer in the flow direction of the fluid to be treated is lengthened to a certain extent.

In addition, in the above-mentioned reaction, damage begins at the catalyst layer near the feedstock hydrocarbon inlet, and in some cases, carbon precipitation occurs, resulting in increased pressure loss.
In a reactor such as that shown in JP-A No. 47-42481, the fluid to be treated is introduced from the upper zone of a multi-stage reaction zone and reaches the lower zone, so that the catalyst in the upper reaction zone, which is most susceptible to damage, is It is not possible to preferentially extract the catalyst, and if it is necessary to extract the catalyst, it has the disadvantage that the undamaged catalyst in the lower reaction zone must also be extracted. .

On the other hand, a reaction zone is provided in a reaction vessel having upper and lower solid particle supply ports and a solid particle discharge port, respectively, and the solid particles loaded in the reaction zone are exchanged during the processing operation of the fluid to be treated. It is also conceivable to use a moving bed type reactor (up-flow type reactor) which has a structure in which the fluid to be treated passes through the reaction zone from bottom to top. In this case, there are various problems such as the loaded solid particles being blown up by the fluid to be treated and being abraded and powdered while flowing in the reaction zone, so it has not been put into practical use yet.

In view of the current situation, the inventors of the present invention conducted extensive research to find out whether there is a reaction device that can eliminate all of the above-mentioned drawbacks, and as a result, they have arrived at the present invention.

That is, the present invention provides a reaction vessel equipped with an inlet and an outlet for a fluid to be treated, and further equipped with an inlet and an outlet for movable solid particles having an activity suitable for treating the fluid to be treated, In a vertical moving bed reactor comprising a plurality of reaction zones loaded with the solid particles arranged in a vertically stacked manner, a) most of the inner and outer surfaces of the reaction zone are treated; A cylindrical lower reaction zone (radial flow type reaction zone) composed of a fluid permeable material, and whose ceiling and bottom surfaces are composed of a fluid impermeable material, and its side surface or most of its side surface. Either it is made of a material that is impermeable to the fluid to be treated, and its ceiling surface is open, or its ceiling surface and/or upper side surface is made of a material that is permeable to the fluid to be treated, and its bottom surface and/or lower side surface is covered. formed by a cylindrical upper reaction zone (down-flow reaction zone) constituted by a permeate of the process fluid, b) said lower reaction zone having a constant distance between its outer surface and the inner wall of the reaction vessel; C) The upper reaction zone has a gap formed in the upper direction of the ceiling surface thereof, and the bottom surface thereof is fixed to the lower part of the reaction vessel, and d) The supply port for the solid particles is connected to the upper end of a supply pipe that penetrates the ceiling of the upper reaction zone. e) the solid particle extraction port is in communication with an opening provided at the bottom of the lower reaction zone via a solid particle extraction pipe; f) the bottom of the upper reaction zone and the ceiling of the lower reaction zone. the surfaces are in communication via a plurality of solid particle transfer conduits, and g) the fluid to be treated is supplied from the inlet for the fluid to be treated from one side of the lower reaction zone to the other side of the cylindrical lower reaction zone. , and then flows out from the outlet of the fluid to be treated without substantially passing through these reaction zones except for passing in a downward flow from the ceiling to the bottom of the upper reaction zone. in the lower reaction zone, characterized in that a baffle plate for controlling the flow direction of the fluid and a fluid transfer cavity for raising the fluid are provided in the reaction vessel. The solid particles loaded in the upper reaction zone and whose activity has deteriorated over time are taken out from the extraction port, and the solid particles loaded in the upper reaction zone are dropped into the lower reaction zone via the solid particle transfer conduit, and further The present invention also provides a vertical moving bed reactor capable of carrying out the series of operations consisting of supplying solid particles with sufficient activity from the supply port during the treatment operation of the fluid to be treated. .

In the reactor, it is preferable that the inlet for the fluid to be treated be provided in the reaction vessel located at a location lower than the ceiling surface of the lower reaction zone; It is desirable that the outlet port is provided in the reaction vessel located higher than the ceiling surface of the lower reaction zone.

The reaction apparatus according to the present invention will be explained in more detail below with reference to FIGS. 1 to 6.

First of all, the present invention provides the introduction port 1 for the fluid to be treated in the side wall of the reaction vessel located lower than the ceiling surface of the lower reaction zone 6A, and also The baffle plate 1 is arranged so as to close the upper end opening of the cavity 7 formed between
2 is arranged so that the fluid to be treated moves upward from the upper end opening of the cavity 14 formed in the inner surface of the lower reaction zone 6A and reaches the ceiling surface of the upper reaction zone 6B. By providing the fluid transfer gap 13, the fluid to be treated supplied into the reaction vessel 5 is allowed to pass across from the outer surface to the inner surface of the cylindrical lower reaction zone 6A, and then to pass through the upper reaction zone 6A. The vertical structure is configured such that the fluid to be treated can flow out from the outlet port 2 without substantially passing through these reaction zones except for passing it in a downward flow from the ceiling surface to the bottom surface of the reaction zone 6B. A moving bed reactor of the type shown in FIG. 1, a specific example of which is shown in longitudinal section, is provided.

Figures 2 and 3 show the reactor shown in Figure 1, respectively.
It shows a cross-sectional view when cut along the AA' line and the B=B' line.

In this case, it is preferable that the inlet 1 for the fluid to be treated is formed of a plurality of inlets, and that each inlet is provided with a fluid dispersion plate (not shown). It is desirable that the outlet 2 be provided on the side wall of the reaction vessel, located higher than the ceiling of the lower reaction zone 6A and lower than the bottom of the upper reaction zone 6B.

Furthermore, in the above-mentioned reaction apparatus, as shown in FIG. The fluid transfer cavity 13 has a lower end opening extended to communicate with the upper end opening of the cavity 14 formed in the inner surface of the lower reaction zone 6A. It is desirable that the center line of the gap be located on or near the center line of the void 14 formed within the inner surface of the lower reaction zone 6A.

Furthermore, the present invention provides the introduction port 1 for the fluid to be treated at the center of the bottom wall of the reaction vessel in the direction of extension of the lower end of the cavity 14 formed in the inner surface of the lower reaction zone 6A. The baffle plate 12 is disposed so as to close the upper end opening of the cavity 14 formed in the inner side of the lower reaction zone 6A, and the baffle plate 12 is disposed so as to close the upper end opening of the cavity 14 formed in the inner side of the lower reaction zone 6A, and the baffle plate 12 is arranged so as to close the upper end opening of the cavity 14 formed in the inner side of the lower reaction zone 6A, and the baffle plate 12 is arranged so as to close the upper end opening of the cavity 14 formed in the inner side of the lower reaction zone 6A. By providing the fluid transfer gap 13 so that the particles to be treated move upward from the upper end opening of the gap 7 formed between the wall and reach the ceiling surface of the upper reaction zone, The fluid to be treated supplied into the reaction vessel 5 is passed across from the inner surface to the outer surface of the cylindrical lower reaction zone 6A, and then passed downward from the ceiling surface to the bottom surface of the upper reaction zone 6B. A vertical moving bed reactor is provided in which the fluid to be treated can flow out from the outlet port 2 without substantially passing through these reaction zones other than in the form of a flow.

Various embodiments can be considered for the reaction apparatus, and typical examples thereof are listed below along with drawings.

First, as an embodiment of the reaction apparatus, a specific example of the longitudinal cross-sectional view of the reaction apparatus is shown in FIG. The upper reaction zone 6B is disposed at a constant interval between the outer surface and the inner wall of the reaction vessel, and the upper and lower open ends of the gap formed therebetween are closed, and the above-mentioned fluid transfer The cavity 13 is formed in the inner surface of the upper reaction zone 6B, and its lower end opening is located on the extension line of the ceiling surface of the lower reaction zone 6A and the bottom surface of the upper reaction zone 6B. It communicates with the upper end opening of the cavity 7 formed between the outer surface of the lower reaction zone 6A and the inner wall of the reaction vessel 5 through the cavity formed between the line and the One example is a vertical moving bed type reactor in which the outlet port 2 for the fluid to be treated is provided in the side wall of the reaction vessel located between the ceiling surface and the bottom surface of the upper reaction zone 6B.

Furthermore, as a second embodiment, a reaction apparatus as shown in FIG. In addition to disposing the upper reaction zone 6B, the gap formed between the extending direction of the ceiling surface of the lower reaction zone 6A and the extending direction of the bottom surface of the upper reaction zone 6B is horizontally separated using the partition plate 16. Furthermore, the fluid transfer cavity 13 is constituted by a cavity formed within the inner surface of the upper reaction zone 6B, and its lower end opening is extended, and its extended end is defined as It communicates with the upper end opening of the cavity 7 formed between the outer surface of the lower reaction zone 6A and the inner wall of the reaction vessel 5 through the lower cavity divided by the partition plate 16. Moreover, there is a vertical moving bed reactor in which the outlet port 2 for the fluid to be treated is provided on the side wall of the reaction vessel located between the bottom surface of the upper reaction zone 6B and the partition plate 16. Moreover, as a third embodiment, a reaction apparatus as shown in FIG. The fluid transfer cavity 13 is formed by arranging the fluid transfer cavity 13 at a constant distance from the wall, and the lower end opening of the fluid transfer cavity 13 is further extended to connect the lower reaction zone 6A and the reaction vessel. The outlet 2 for the fluid to be treated is provided in the center of the ceiling wall of the reaction vessel 5, communicating with the upper end opening of the cavity 7 formed between the inner wall and the outlet 2. The upper end opening of the cavity formed in the inner surface of the upper reaction zone 6B is extended to communicate with the upper end opening of the cavity, and the ceiling surface of the lower reaction zone 6A and the upper reaction zone 6B are connected to the lower end opening of the cavity. An example is a vertical moving bed reactor in which a gap formed between the reactor and the bottom is communicated.

However, as mentioned above, these embodiments show typical specific examples of the above-mentioned reaction apparatus according to the present invention, and it goes without saying that the present invention is not limited to these embodiments. be.

Similarly, in these reactors, that is, in the reactor equipped with the embodiments described above, the inlet 1 for the fluid to be treated is formed of a single lower reaction zone whose center line extends in the vertical direction. The cavity 14 formed in the inner surface of 6A has a plurality of dispersed particles. Preferably, a fluid distributor consisting of 17 is provided.

In this case, the fluid distributor may include a plurality of hollow dispersion plates 17A arranged at appropriate intervals, and plate-shaped dispersion plates 17B arranged at appropriate intervals. It is particularly desirable to have a structure in which the fluid distributor is held by a support (not shown), and such a fluid distributor is usually attached such that the hollow distribution plate 17A is located on the inlet 1 side of the fluid to be treated.

As described above, the reaction apparatus according to the present invention is roughly divided into two types depending on the position of the introduction port 1 for the fluid to be treated.
Moreover, as described above, each of these reactors has its own preferred embodiments, but other preferred embodiments that can be applied to all of these reactors are as follows.

1. Each of the reaction zones 6 has one upper reaction zone 6.
The above-mentioned moving bed reactor comprises a lower reaction zone 6A and a lower reaction zone 6A, each of which has a cylindrical shape.

2. The moving bed reactor described above, wherein the opaque body constituting the reaction zone 6 is a metal plate or a plastic plate.

3. The moving bed reactor described above, wherein the permeable body constituting the reaction zone 6 is a wire mesh or a perforated plate having a mesh smaller than the particle size of the solid particles, for example, a mesh having a mesh size of one-half or less of the particle size. .

4. The solid particle transfer conduit 11 is an elongated conduit having a diameter smaller than the diameter of the inlet/outlet of the fluid to be treated.
The aforementioned moving bed reactor.

5. The diameter of the solid particle transfer conduit 11 is selected from a range of 15 to 100 mm, and the length thereof is selected so that the treated fluid does not short-circuit between the upper reaction zone 6B and the lower reaction zone 6A through the conduit. 5. A moving bed reactor according to claim 4, wherein the length of the conduit is at least longer than the distance between the inner and outer surfaces of the lower reaction zone.

6. An opening is provided in the middle of the solid particle transfer conduit, and a sealing fluid supply tube 18 is connected to the opening, so that the fluid to be treated is supplied to the upper reaction zone 6 through the solid particle transfer conduit 11.
5. The moving bed reactor according to item 4, wherein there is no flow between B and the lower reaction zone 6A.

7. The sealing fluid is at least connected to the outlet port 2 for the fluid to be treated.
7. The moving bed reactor according to item 6, wherein the fluid to be treated is discharged from the moving bed reactor.

8. In the moving bed reactor described above, the solid particle transfer conduit 11 and the ceiling surface of the lower reaction zone 6A are connected by an expansion joint 19.

9. A truncated cone-shaped deflection device 20 is attached to the solid particle layer in the upper reaction zone 6B located above the solid particle transfer conduit 11.
said moving bed reactor, comprising: providing a moving bed reactor to facilitate the movement of solid particles from the upper reaction zone 6B to the lower reaction zone 6A.

10. The upper side surface 21 of the lower reaction zone 6A is made of an impermeable material, and the vertical length of the impermeable material is equal to the length of the entry portion of the solid particle transfer conduit 11 extending into the reaction zone. By making the length longer than the length, the fluid to be treated introduced from the inlet port 1 of the fluid to be treated flows into the lower reaction zone 6.
The moving bed reactor described above is prevented from flowing from one side of the reaction zone 6A to the other side without passing through the solid particle layer in A.

11. The moving bed reactor described above, wherein the solid particles are catalysts or adsorbents in the form of spheres or pellets.

12. In the moving bed reactor described above, the permeable body constituting the ceiling surface of the upper reaction zone 6B is a perforated plate having a function of allowing the fluid to be treated to flow uniformly into the upper reaction zone 6B.

13. The solid particle feed port 3 of the moving bed reactor is connected to a conventional solid particle feed device, such as a lock hopper, consisting of a single droplet.

14. In the moving bed reactor, the solid particle extraction port 4 is connected to a conventionally known solid particle extraction device, for example, the device described in JP-A No. 50-26757.

Next, the mode of use of the above-mentioned reaction apparatus according to the present invention will be explained.

Typical usage forms of the reaction apparatus according to the present invention include reaction apparatuses for hydrotreating or hydrocracking processes for light or heavy hydrocarbons, and further for steam reforming processes.

However, the reactor also handles the fluid to be treated.
It can be used as a reactor for processes that require continuous treatment over a long period of time without interrupting the treatment operation.

For example, there are reactors for removing sulfur contained in hydrocarbons such as naphtha in the presence of desulfurization adsorption catalysts such as iron oxide and zinc oxide, and sulfur oxides and/or substances contained in flue gas such as combustion exhaust gas. It is not only applied to reaction equipment, etc. for removing harmful components of nitrogen oxides in the presence of a desulfurization catalyst and/or denitrification catalyst, but also for removing impurities contained in an aqueous solution in the presence of an adsorbent such as activated carbon. It can also be used as a reaction device for adsorption and removal.

Furthermore, if an inlet for a second fluid to be treated is provided in the middle of the fluid transfer gap 13 in the reactor, and the raw material hydrocarbon is also introduced from this inlet, the raw material hydrocarbon It can also be used as a reactor for two-stage steam reforming reactions.

Hereinafter, an example will be shown in which a steam reforming reaction of raw material hydrocarbon for city gas production was carried out using the reaction apparatus shown in FIG. 5 (auxiliary equipment not shown).

Example After loading a low-temperature steam reforming catalyst in the form of pellets of 2 mm diameter supported on nickel silica-alumina into the reaction zones 6A and 6B of FIG. , FBP 1 2 2℃, d4
0.675 and C6. .

Mixture of raw material hydrocarbon vapor and steam having properties of 4H13.4 (mixing ratio H20/c=2.0) 4
9. Preheat to a temperature of 0°C and introduce. 14. 5k
When the steam reforming reaction was carried out under the pressure condition of g/crttG, CH
45 5. 3 vol%H2 2 1. 4 vo
l%, Co0. 9 vol% and C0222.
A gas mixture consisting of 4 vol % was obtained.

In this case, the fluid to be treated is introduced from the inlet 1 and is evenly distributed by colliding with the distribution plates 17A and 17B and the baffle plate 12, etc., from the inner surface to the outer surface of the lower reaction zone 6A. direction and then ascends through the fluid transfer cavity 13 to form the cavity 8 in the upper part of the reaction vessel.
The fluid then passes from the ceiling to the bottom of the upper reaction zone 6B and is finally discharged from the outlet port 2 for the fluid to be treated. It was observed that an endothermic reaction based on the methane production occurred, and the outlet temperature of the catalyst layer was approximately 442°C. Furthermore, in the upper reaction zone 6B, an exothermic reaction based on the methane production reaction occurred. It was observed that the temperature at the outlet of the catalyst layer was about 496°C.

After carrying out the steam reforming reaction continuously for about 10 hours, assuming that an erroneous operation occurred in the above operation, only the amount of steam was reduced and the mixing ratio H20/c was adjusted to 1.6.
When the pressure loss increased, the mixing ratio was returned to the original value and the operation was continued, but it was still observed that the pressure loss gradually increased, so the upper reaction zone 6B and A small amount of each catalyst was sampled from the lower reaction zone 6A and its activity etc. were measured.

As a result, it was found that the catalyst loaded in the upper reaction zone 6B had almost the same activity as the catalyst at the time of loading, but the catalyst loaded in the lower reaction zone It was found that the catalyst was considerably damaged, and that carbon was deposited on the catalyst, clogging the catalyst bed.

This seems to be due to abnormal decomposition of the raw material hydrocarbon in the catalyst layer of the lower reaction zone 6A, but this can be confirmed by replacing only the catalyst loaded in the lower reaction zone 6A. This suggests that it can be carried out continuously over a period of time.

Therefore, while conducting the operation related to the steam reforming reaction mentioned above,
When the catalyst loaded in the lower reaction zone 6A was removed from the solid particle extraction port 4 and a new catalyst was supplied from the solid particle supply port 3 to replace the catalyst, the pressure loss was reduced. The reactor returned to steady operation, and thereafter was able to carry out smooth steam reforming reactions without any problems.

As mentioned above, according to the vertical mobile reactor according to the present invention, it is possible to replace the solid particles such as the catalyst and adsorbent loaded in the reactor during the treatment operation of the fluid to be treated. It is extremely economical because the fluid to be treated can be treated continuously over a long period of time, and only solid particles that have lost their activity can be preferentially replaced.

[Brief explanation of the drawing]

1 and 4 to 6 are vertical sectional views showing a specific example of the vertical moving bed reactor according to the present invention, and FIGS. 2 and 3 are longitudinal sectional views of the reaction apparatus shown in FIG. 1. FIG. 3 shows cross-sectional views taken along the AA' line and the BB' line, respectively. 1... Inlet for fluid to be treated, 2... Outlet for fluid to be treated, 3... Supply port for solid particles,
4...Solid particle extraction port, 5...Reaction vessel, 6A...Lower reaction zone, 6B...
- Upper reaction zone, 7, 8, 14... ．． ...Void part, 9
......Solid particle supply pipe, 10...Solid particle extraction pipe, 11...Solid particle transfer pipe,
12... Baffle plate, 13... Fluid transfer gap, 16... Partition plate, 17A, 17B...
... Dispersion plate, 18 ... Seal fluid supply pipe, 2
0...Deflection device.

Claims (1)

[Scope of Claims] 1. A reaction vessel equipped with an inlet and an outlet for a fluid to be treated, and further equipped with an inlet and an outlet for movable solid particles having an activity suitable for treating the fluid to be treated. In a vertical moving bed reactor comprising a plurality of reaction zones loaded with the solid particles stacked vertically, a). The reaction zone has a cylindrical lower reaction zone whose inner and outer surfaces are mostly composed of a permeable body for the fluid to be treated, and further whose ceiling and bottom surfaces are composed of an impermeable body for the fluid to be treated; Most of the side surfaces are made of an impermeable material for the fluid to be treated, and the ceiling surface is left open, or the ceiling surface and/or the upper side surface is made of a material that is permeable to the fluid to be treated. b) the lower reaction zone is formed by a cylindrical or columnar upper reaction zone whose bottom surface and/or lower side surface is composed of a permeate of the fluid to be treated; b) the lower reaction zone has an outer surface thereof and an inner wall of the reaction vessel; C) The upper reaction zone has voids formed in the upper direction of its ceiling surface, and the bottom surface of the upper reaction zone is fixed to the lower part of the reaction vessel. , and is attached at a constant distance between the bottom surface and the ceiling surface of the lower reaction zone, and d) the supply port for the solid particles is located at the upper end of a supply pipe that penetrates the ceiling surface of the upper reaction zone. e) the solid particle extraction port communicates with an opening provided at the bottom of the lower reaction zone via a solid particle extraction pipe; f) the bottom of the upper reaction zone and The ceiling surface of the lower reaction zone is communicated via a plurality of solid particle transfer conduits, and g) The fluid to be treated supplied from the inlet for the fluid to be treated is connected to the cylindrical lower reaction zone. The fluid to be treated does not substantially pass through these reaction zones except for passing across from one side to the other and then passing in a downward flow from the ceiling to the bottom of the upper reaction zone. The reaction vessel is characterized in that a baffle plate for controlling the flow direction of the fluid and a fluid transfer gap for raising the fluid are provided in the reaction vessel so that the fluid can flow out from the outlet of the reaction vessel. The solid particles loaded into the lower reaction zone and which have deteriorated over time are taken out from the outlet, and the solid particles loaded into the upper reaction zone are transferred into the lower reaction zone through the solid particle transfer conduit. A vertical moving bed reactor capable of carrying out a series of operations during the processing operation of the fluid to be treated, consisting of dropping solid particles into the fluid and supplying solid particles with sufficient tongue performance from the supply port. 2. The apparatus according to claim 1, wherein the inlet for the fluid to be treated is provided in a reaction vessel located lower than the ceiling surface of the lower reaction zone. 3. The apparatus according to claim 1, wherein the outlet for the fluid to be treated is provided in a reaction vessel located higher than the ceiling surface of the lower reaction zone. 4. An inlet for the fluid to be treated is provided in the side wall of the reaction vessel located lower than the ceiling surface of the lower reaction zone, and is formed between the outer surface of the lower reaction zone and the inner wall of the reaction vessel. The baffle plate is disposed so as to close the upper end opening of the void formed in the lower reaction zone, and the fluid to be treated moves upward from the upper end opening of the void formed within the inner surface of the lower reaction zone. By providing the fluid transfer gap so as to reach the ceiling surface of the upper reaction zone,
Passing the fluid to be treated supplied into the reaction vessel from the outer surface to the inner surface of the cylindrical lower reaction zone,
Next, the fluid to be treated can flow out from the outlet of the fluid to be treated without substantially passing through these reaction zones except for passing it in a downward flow from the ceiling surface to the bottom surface of the upper reaction zone. An apparatus according to claim 1. 5. The apparatus according to claim 4, wherein the inlet for the fluid to be treated is comprised of a plurality of inlets, and each inlet is biased by a fluid dispersion plate. 6. The fluid transfer cavity is constituted by a cavity formed within the inner surface of a cylindrical upper reaction zone whose outer surface is in close contact with the inner wall of the reaction vessel, and whose lower end opening is extended. communicating with the upper end opening of the cavity formed in the inner surface of the lower reaction zone, and the centerline of the fluid transfer cavity is on the centerline of the cavity formed in the inner surface of the lower reaction zone; 5. The device according to claim 4, wherein the device is located at or in the vicinity thereof. 7. The outlet for the fluid to be treated is provided in a side wall of the reaction vessel located higher than the ceiling surface of the lower reaction zone and lower than the bottom surface of the upper reaction zone. An apparatus according to claim 4. 8. An inlet for the fluid to be treated is provided at the center of the bottom wall of the reaction vessel in the direction of extension of the lower end of the cavity formed within the inner surface of the lower reaction zone, and an inlet for the fluid to be treated is provided within the inner surface of the lower reaction zone. The baffle plate is arranged so as to close the upper end opening of the cavity formed between the outer surface of the lower reaction zone and the inner wall of the reaction vessel. By providing the fluid transfer gap section so that the fluid to be treated moves upward from the upper reaction zone and reaches the ceiling surface of the upper reaction zone, the fluid to be treated supplied into the reaction vessel is transferred to the cylindrical lower section. The reactor is not allowed to pass substantially through these reaction zones except for passing it transversely from the inner side to the outer side of the reaction zone and then in a downward flow from the ceiling to the bottom of said upper reaction zone. 2. The apparatus according to claim 1, wherein the processing fluid is allowed to flow out from the outlet. 9 The above-mentioned inlet for the fluid to be treated is composed of a single inlet, and the gap formed in the inner surface of the lower reaction zone whose center line extends in the vertical direction is composed of a plurality of dispersion plates. 9. Device according to claim 8, characterized in that it is equipped with a fluid distributor. 10 The above fluid distributor is one in which a plurality of hollow dispersion plates are arranged at appropriate intervals, and plate-shaped dispersion plates are further arranged at appropriate intervals, and the hollow dispersion plates are arranged at appropriate intervals. 10. The apparatus according to claim 9, wherein the apparatus is attached so as to be located on the inlet side of the fluid to be treated. 11 A cylindrical upper reaction zone having an outflow portion for the fluid to be treated at the lower part of the outer surface thereof is disposed at a constant interval between the outer surface and the inner wall of the reaction vessel, and a cylindrical upper reaction zone is formed therebetween. The upper and lower opening ends of the cavity are closed, and the fluid transfer cavity is constituted by a cavity formed within the inner surface of the upper reaction zone, and the lower end opening is closed to the ceiling surface of the lower reaction zone. and the upper end of the gap formed between the outer surface of the lower reaction zone and the inner wall of the reaction vessel through the gap formed between the extension line of the lower reaction zone and the extension line of the bottom surface of the upper reaction zone. Claim 8, characterized in that an outlet for communicating with the opening and for the fluid to be treated is provided in a side wall of the reaction vessel located between the ceiling surface and the bottom surface of the upper reaction zone. equipment. 12. A cylindrical upper reaction zone having the outflow portion of the fluid to be treated on the bottom surface and whose outer surface is in close contact with the inner wall of the reaction vessel is provided, and the upper reaction zone is arranged in the extending direction of the ceiling surface of the lower reaction zone. The gap formed between the extending direction of the bottom surface of the upper reaction zone is horizontally divided by a partition plate, and the fluid transfer gap is further formed within the inner surface of the upper reaction zone. The outer surface of the lower reaction zone and the reaction vessel are connected to each other through the lower cavity, which is formed by a cavity, and whose lower end opening is extended, and whose extended end is divided by the partition plate. A side wall of the reaction vessel communicating with the upper end opening of the gap formed between the inner wall of the reaction vessel and having an outlet for the fluid to be treated located between the bottom surface of the upper reaction zone and the partition plate. 9. The device according to claim 8, characterized in that it is provided in a. 13 The cylindrical upper reaction zone having the outflow portion of the fluid to be treated at the bottom thereof is disposed with a constant distance between the outer surface of the upper reaction zone and the inner wall of the reaction vessel, thereby forming the fluid transfer gap. furthermore, the lower end opening of the fluid transfer cavity is extended to communicate with the upper end opening of the cavity formed between the lower reaction zone and the inner wall of the reaction vessel; A fluid outlet is provided in the center of the ceiling wall of the reaction vessel, and the upper end opening of the gap formed in the inner surface of the upper reaction zone is extended and communicated with the outlet. 9. The apparatus according to claim 8, wherein the lower end opening communicates with a gap formed between the ceiling surface of the lower reaction zone and the bottom surface of the upper reaction zone. 14. The apparatus of claim 1, wherein each of said reaction zones comprises an upper reaction zone and a lower reaction zone, each of which is cylindrical in shape. 15. The apparatus according to claim 1, wherein the opaque body constituting the reaction zone is made of a metal plate or a plastic plate. 16. The apparatus according to claim 1, wherein the permeable body constituting the reaction zone is a wire mesh or a perforated plate having a mesh smaller than the particle size of the solid particles. 17. The apparatus according to claim 1, wherein the solid particle transfer conduit is an elongated conduit having a diameter smaller than the diameter of the inlet and outlet of the fluid to be treated. 18. The apparatus of claim 17, wherein the length of the solid particle transfer conduit is at least greater than the spacing between the inner and outer surfaces of the lower reaction zone. 19 An opening is provided in the middle of the solid particle transfer conduit, and a sealing fluid supply tube is connected to the opening, so that the fluid to be treated passes between the upper reaction zone and the lower reaction zone through the solid particle transfer conduit. 18. The device according to claim 17, wherein the device is not distributed. 20. The apparatus according to claim 19, wherein the sealing fluid is at least a fluid to be treated discharged from an outlet for the fluid to be treated. 21. A truncated cone-shaped deflection device is provided in the solid particle layer in the upper reaction zone located above the solid particle transfer conduit to facilitate the movement of solid particles from the upper reaction zone to the lower reaction zone. An apparatus according to claim 1. 22. The device according to claim 1, wherein the solid particles are catalysts or adsorbents. 23. The apparatus according to claim 1, wherein the fluid to be treated comprises a gaseous fluid or a vaporous fluid.