CN109985575B

CN109985575B - Hydrogenation reactor with impact reduction assembly

Info

Publication number: CN109985575B
Application number: CN201811291429.5A
Authority: CN
Inventors: 王璐瑶; 彭德强; 刘杰
Original assignee: China Petroleum and Chemical Corp; Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Current assignee: Sinopec Dalian Petrochemical Research Institute Co ltd; China Petroleum and Chemical Corp
Priority date: 2017-12-29
Filing date: 2018-10-31
Publication date: 2021-08-31
Anticipated expiration: 2038-10-31
Also published as: CN109985575A

Abstract

The invention discloses a hydrogenation reactor with an impact reduction assembly. The hydrogenation reactor comprises a material inlet pipe, an inlet diffuser, a reactor upper end enclosure, an impact reduction flow equalizing disc, a catalyst bed layer, a catalyst support grid, a reactor barrel, a reactor lower end enclosure, an outlet collector, a material outlet pipe and an agent unloading pipe. The impact reduction and flow equalization disc is arranged in the idle space of the upper end socket of the reactor or at the upper end of the cylinder body of the reactor; the impact reducing and flow equalizing disc comprises an impact reducing tray and a plurality of distributors arranged on the impact reducing tray, each distributor comprises a grid, a material dropping pipe and a connecting rod, the grids are arranged above the material dropping pipes, and the grids are connected with the material dropping pipes through the connecting rods. The hydrogenation reactor is suitable for hydrogenation reaction process, especially for hydrogenation refining or hydrocracking process with large scale reactor.

Description

Hydrogenation reactor with impact reduction assembly

Technical Field

The invention relates to a hydrogenation reactor with an impact reduction assembly, and belongs to the field of chemical equipment. The hydrogenation reactor is suitable for hydrogenation reaction process, especially for hydrogenation refining or hydrocracking process with large scale reactor.

Background

In recent years, with the rapid development of economy and the enhancement of environmental awareness, the quality and environmental protection requirements of petrochemicals are higher and higher. As a technical means for producing clean fuels, the importance and role of hydrogenation technology in the oil refining industry is increasing. In the hydrogenation device, as with the hydrogenation catalyst technology and the hydrogenation process technology, the hydrogenation reactor technology is an important component of the reactor system, and the three components form three factors of the performance of the reactor. In a hydrogenation device, raw oil which is taken as key equipment of a hydrogenation reactor is mixed with hydrogen according to a certain proportion, and refining, cracking and other reactions are finished in the raw oil under the action of a hydrogenation catalyst. Whether the hydrogenation reaction in the hydrogenation reactor can be stably operated or not, whether the hydrogenation catalyst can fully exert the function or not, whether the product quality can reach high quality or not, and the method depends on the uniformity of the distribution of gas and liquid in a catalyst bed layer to a great extent. Whether the gas and liquid are uniformly distributed in the catalyst bed layer or not is closely related to the design of the internal components of the hydrogenation reactor. In other words, the performance of the internals directly affects the catalyst life, product quality and the operation period of the apparatus, i.e. the effect obtained by using a set of excellent-performance internals in the hydrogenation process is in no way inferior to that obtained by using a more active catalyst. Therefore, the research and engineering development of hydrogenation reactors and internal components thereof at home and abroad are always very important, and the internal components of the reactors are continuously updated to obtain better effect.

The production practice of industrial devices shows that two factors are mainly used for restricting the stable operation of a hydrogenation process device, one is larger radial temperature difference of a reactor caused by uneven material distribution, and the other is abnormal shutdown caused by too fast pressure drop of a catalyst bed layer of the reactor.

The hydrogenation reactor feeds materials at the center of the top of the reactor, and although an inlet diffuser is arranged, the residual kinetic energy of material conveying can generate strong impact force; another flow regime characteristic of central point position feeding is that the streamline of material in the formation of reactor head space is the tilt line, the kinetic energy of material and the flow regime that is the tilt line, with the liquid layer on top distributor tray to the reactor rush to send all around, form the "push away unrestrained" phenomenon of material on top distributor tray, promptly, reactor distributor tray is from the central point to the liquid layer height of border position and is incremental type distribution: the material liquid layer in the central area is small and even has no liquid layer, and the height of the material liquid layer on the side wall of the reactor is the largest, so that unfavorable inlet conditions are brought to a distributor depending on the levelness of a tray, and even the distributor with the best performance can not realize uniform distribution of materials under the conditions of the liquid layers with different heights. Along with the increasing scale of the hydrogenation reactor, the 'push wave' phenomenon generated by the impact force formed by the conversion of residual kinetic energy and potential energy of the material after entering the reactor is more and more serious, so that the material distribution has serious deviation.

The hydrogenation process is an exothermic reaction, and uneven material distribution can cause severe reaction at the part with good catalyst wetting effect and generate more heat; i.e. the radial temperature difference affecting the reactor. When the radial temperature difference is large, the higher the local temperature of the catalyst is, the faster the reaction rate is, hot spots are formed, the performance of the catalyst is inactivated too early, the performance of the catalyst is damaged, even coking and hardening of a part of regions of the catalyst can be caused, materials can not flow normally, and the catalyst below the hardening region can not play a role due to the fact that the fixed bed hydrogenation reactor is in a trickle bed flow state, so that the service life of the catalyst is greatly prolonged, and the start-up period of the device is greatly shortened. Localized sheeting also causes an increase in the pressure drop across the catalyst bed, which increases the operating pressure of the reactor to continue operation, resulting in increased energy consumption.

With the increasing enlargement of the scale of hydrogenation reactors, the product precision requirement is increased, and the uniform distribution of materials on a catalyst bed layer is very important. Because the hydrogenation process is an exothermic reaction, raw oil is unevenly distributed on the radial section of a catalyst bed, so that radial temperature difference is generated due to different reaction degrees, even local overheating occurs, and the performance of the catalyst is damaged, thereby greatly reducing the service cycle of the catalyst. Therefore, it is necessary to select a hydrogenation reactor with reasonable design.

Disclosure of Invention

In view of the deficiencies in the prior art, the present invention provides a hydrogenation reactor having an impact reduction assembly.

The hydrogenation reactor with the impact reduction assembly comprises a material inlet pipe, an inlet diffuser, a reactor upper end enclosure, an impact reduction flow equalizing disc, a catalyst bed layer, a catalyst support grid, a reactor barrel, a reactor lower end enclosure, an outlet collector, a material outlet pipe and an agent unloading pipe; the impact reduction and flow equalization disc is arranged in the idle space of the upper end socket of the reactor or at the upper end of the cylinder body of the reactor; the impact reducing and flow equalizing disc comprises an impact reducing tray and a plurality of distributors arranged on the tray, each distributor comprises a grid, a material dropping pipe and a connecting rod, the grids are arranged above the material dropping pipes, and the grids are connected with the material dropping pipes through the connecting rods. The flow reducing and equalizing disc has the characteristics of flow reducing and equalizing functions, good distribution effect, small size, low requirement on installation precision and the like.

In certain embodiments, the hydrogenation reactor of the present invention further comprises a bed unloading agent tube, a cold hydrogen tray, an injection tray, an interbed distribution tray. I.e. the hydrogenation reactor comprises more than two hydrogenation catalyst beds.

In a further preferred embodiment, the hydrogenation reactor of the present invention further comprises a top distribution tray located below the flow reduction and equalization tray.

In the impact-reducing flow-equalizing disc, a space is formed between the lower surface of the grid and the uppermost edge of the material dropping pipe, and the space forms a flow channel of gas-phase materials.

Furthermore, the outermost edge of the tray is provided with a folding edge which is upward in direction and has a certain height. The tray can be divided into a plurality of small trays, and the small trays can be assembled into a whole tray.

Furthermore, the grating comprises a plurality of grating plates and grating plate connecting rods, and the plurality of grating plates are connected together through the grating plate connecting rods. The plurality of grating plates are arranged in parallel in the horizontal direction and are obliquely arranged. The inclination direction of the grating plate is the outer edge direction of the reactor, and the inclination angle of the grating plate is 10-90 degrees, preferably 20-45 degrees. The width of the grating plate is 10-200 mm, preferably 50-120 mm; the (horizontal) distance between adjacent grating plates is 10-300 mm, preferably 50-150 mm. The grid formed by the parallel arrangement of the plurality of grid plates in the horizontal direction is rectangular or cut into a circle.

Furthermore, the distributors are arranged on the tray according to a certain rule and are arranged in a triangular shape, a quadrilateral shape, a diamond shape or a circular shape.

Further, the distributor and the tray can be welded, bolted, screwed or fastened, preferably bolted.

Further, the number of the grids and the number of the material dropping pipes are the same or different, and are preferably the same.

Furthermore, a certain number of overflow holes are formed in the material descending pipe, and a certain height is formed between the center line of each overflow hole and the upper surface of the tray.

Furthermore, when the grid type flow reducing and equalizing disc is arranged at the upper end of the reactor barrel, the grid type flow reducing and equalizing disc is preferably arranged above the topmost distribution disc in the reactor.

Compared with the prior art, the hydrogenation reactor with the impact reduction assembly has the following advantages:

1. the invention provides the concept of arranging a novel reactor inner member of a grid type impact reduction and flow equalization disc in a reactor for the first time, wherein the grid type impact reduction and flow equalization disc is a newly added reactor inner member and can reduce the strong impact force formed by residual kinetic energy when materials enter the reactor; the 'wave pushing' effect of materials in an inclined flow state on a liquid layer on a distribution disc at the top in the reactor, which is caused by the adoption of the existing central feeding mode, is eliminated; eliminating the impact force of the liquid material falling from the inlet of the reactor to the top distribution plate and converted from potential energy; fine adjustment of the fluid state of the liquid material fluid is realized; realize the initial distribution of the materials. The grid type flow reducing and equalizing disc can also replace the distribution function of the top distribution disc, and can provide good inlet conditions for a top catalyst bed layer. The newly added grid type impact-reducing and flow-equalizing disc has the advantages of impact-reducing and flow-equalizing functions, good distribution effect, small volume, low requirement on installation precision and the like.

2. According to the hydrogenation reactor, the impact reduction flow equalizing disc is provided with the distributor with the impact reduction function, the grid at the upper part of the distributor can block the jet fluid which is in an inclined flow state and is formed by adopting a central feeding mode, the impact force generated by the fact that the fluid falls from the inlet of the reactor to the distribution disc at the top part and is converted from potential energy is eliminated, the fluid losing kinetic energy falls under the action of gravity after being blocked, the original inclined flow state is converted into a vertical flow state, the natural effect is realized, and the phenomenon of 'wave pushing' of the material to a liquid layer on the distribution disc is eliminated. The fluid falls on the tray to form a liquid layer with consistent depth, so that friendly, stable and uniform inlet conditions are provided for the catalyst bed layer or the top distributor, and fine adjustment of fluid flow state and initial distribution of materials are realized. The grid type impact reducing and flow equalizing disc which is suitable in quantity and has the impact reducing function is arranged, the existing top distribution disc can be replaced, and the uniform distribution function of materials is realized.

3. In the hydrogenation reactor, the uniform distribution of the liquid phase is realized through the arranged impact reduction and flow equalization discs, and compared with a bubble cap distributor based on the traditional suction principle, the dispersed power of the liquid phase distribution is changed from gas phase suction to potential energy to form splashing, so that the pressure drop is reduced.

4. According to the hydrogenation reactor, the overflow holes with proper shapes are arranged at proper positions on the pipe wall of the descending pipe, so that a liquid layer with a certain reasonable depth is formed and exists on the tray, and the macro-distribution unevenness caused by the levelness deviation and the liquid level fluctuation of the tray is reduced.

5. The hydrogenation reactor of the invention adopts unique design principle and fluid mechanics characteristics to realize uniform distribution of materials, and particularly can reduce radial temperature difference of a catalyst bed when being applied to catalytic reaction of a reactor filled with catalyst, the radial temperature difference of the catalyst bed is not more than 3 ℃, and the radial temperature difference reflects the distribution effect of fluid, so that the invention fully shows that the tooth weir type flow-equalizing disc has good distribution effect on reaction feed material flow and gas-liquid mixing effect, and has certain auxiliary effect on catalytic reaction process and catalyst coking control.

6. Compared with the prior art, the hydrogenation reactor with the impact reducing assembly has the advantages that the impact reducing and flow equalizing disc is simple in structure, convenient to install and high in operation elasticity, can be installed in the upper end socket of the reactor or arranged at the upper end of the cylinder body of the reactor and above the top distribution disc, can improve the space utilization rate of the reactor, and is convenient to fill more catalysts and other equipment in the reactor or reduce the scale of the reactor. The method has the advantages of improving the inlet condition of the top material of the reactor, improving the radial distribution effect of the feeding of the reactor, effectively eliminating the radial temperature difference of the reactor, eliminating the hot spot caused by uneven material distribution of the catalyst bed layer, providing excellent inlet condition for the effective use of the catalyst in the reactor, reducing the number of times of catalyst head skimming or agent changing, prolonging the start-up period of the device, improving the process effect and having good economic benefit.

Drawings

FIG. 1 is a schematic diagram of the structure of a hydrogenation reactor of the present invention.

Fig. 2 is a schematic diagram of the reduced-impulse flow equalization panel of the present invention.

Fig. 3 is a schematic view of a distributor of the flow reducing and equalizing disc of the present invention.

Fig. 4 is a diagram of the current equalizing disc of the impact reducing current equalizing disc of the present invention.

Fig. 5 is a schematic view of the flow direction of liquid when the flow reducing and equalizing disc works.

FIG. 6 is a schematic view showing the positions of different temperature measuring points on the same bed section in the example of the present invention and the comparative example.

Detailed Description

The embodiments of the present invention will be described in further detail with reference to the drawings and examples. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.

In the description of the present invention, it is to be noted that, unless otherwise specified, "a plurality" means one or more than one, and "a plurality" means two or more than two; the terms "upper", "lower", "inner", "outer", "top", "bottom", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience in describing and simplifying the description, but do not indicate or imply that the referred devices or elements must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.

In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; may be directly connected or indirectly connected through an intermediate. The specific meaning of the above terms in the present invention can be understood as appropriate to those of ordinary skill in the art.

As shown in fig. 1 to 4, the hydrogenation reactor of the present invention comprises a material inlet pipe 1, an inlet diffuser 2, a reactor upper head 3, a flow reduction and equalization disc 4, a catalyst bed 5, a catalyst support grid 6, a reactor barrel 12, a reactor lower head 13, an outlet collector 14, a material outlet pipe 15, an agent discharge pipe 16 and a support 18. In certain embodiments, the hydrogenation reactor further comprises a bed unloading agent pipe 7, a cold hydrogen pipe 8, a cold hydrogen tray 9, an injection tray 10, and an interbed distribution tray 11, i.e., the hydrogenation reactor comprises more than two catalyst beds. In yet a further preferred embodiment, the hydrogenation reactor of the present invention further comprises a top distribution tray 17, the top distribution tray 17 being located below the reduced flow equalization tray.

The impact reduction and flow equalization plate 4 comprises an impact reduction tray 4-2, a tray connecting piece 4-3 and a distributor 4-1 arranged on the impact reduction tray; the distributor 4-1 comprises a grid 4-1-1, a material dropping pipe 4-1-4 and a connecting rod 4-1-3, the grid 4-1-1 is arranged above the material dropping pipe 4-1-4, and the grid 4-1-1 is connected with the material dropping pipe 4-1-4 through the connecting rod 4-1-3. And a space exists between the lowest edge of the grid 4-1-1 and the uppermost edge of the blanking pipe 4-1-4, and the space forms a flow channel of gas-phase materials. The space height is 5-200 mm, preferably 10-50 mm, and the outermost edge of the tower tray 4-2 is provided with an upward folded edge 4-4. The height of the folded edge is 5-80 mm, and preferably 30-50 mm. The grating 4-1-1 comprises grating plates 4-1-6 and grating plate connecting rods 4-1-2, a plurality of grating plates 4-1-6 are connected together through the grating plate connecting rods 4-1-2, the grating plates 4-1-6 are arranged in parallel in the horizontal direction, the grating plates 4-1-6 are arranged in an inclined mode, and the inclined direction is towards the outer edge direction of the reactor. The inclination angle of the grating plate 4-1-6 is generally 10-90 degrees, and preferably 20-45 degrees. The width of the grid plate 4-1-6 is 10-200 mm, preferably 50-120 mm. The distance between the adjacent grating plates 4-1-6 is 10-300 mm, preferably 50-150 mm. The number of the grids 4-1-1 and the number of the material dropping pipes 4-1-4 are the same or different, and are preferably the same. The material dropping pipe 4-1-4 is provided with an overflow hole 4-1-5. The number of the overflow holes 4-1-5 is 1-6, and preferably 1-2. The total cross-sectional area of the overflow holes 4-1-5 is 10% -100% of the cross-sectional area of the material descending pipe 4-1-4, and preferably 30% -50%. The shape of the overflow holes 4-1-5 is polygonal, specifically triangular, quadrangular or circular, preferably circular. The center line of the overflow hole 4-1-5 is 5-100 mm, preferably 30-50 mm away from the upper surface of the tower tray. The distributor 4-1 and the tray 4-2 are welded, bolted, screwed or snap-fit, preferably bolted. The distributors 4-1 are arranged on the tray 4-2 according to a certain rule and are arranged in a triangular shape, a quadrangular shape, a rhombic shape or a circular shape. The impact reduction and flow equalization disc 4 is arranged in an upper end enclosure of the reactor or at the upper end of a cylinder body of the reactor; when disposed at the upper end of the reactor barrel, it is preferably disposed within the reactor above the topmost distribution tray. The lower end of the downcomer is inserted on the shock-reducing tower tray and is fixedly connected with the shock-reducing tower tray, and the tail end of the downcomer is flush with or extends out of the shock-reducing tower tray.

As shown in fig. 5, the working process of the flow reduction equalizing disc in the hydrogenation reactor of the present invention is further explained with reference to fig. 1 to 4: when the impact reducing and flow equalizing disc works, materials enter the reactor from an inlet diffuser of the reactor, and have residual kinetic energy due to the mechanical pump conveying, so that the materials have strong impact force. Because the material is fed from the center of the reactor, the material is still sprayed to the periphery in an oblique line flow state although the existing reactors are all provided with inlet diffusers. After the tooth weir type impact reduction flow equalizing disc provided by the invention is arranged in a reactor, fluid firstly impacts the grid 4-1-1 of the distributor 4-1, the fluid sprayed in a diagonal flow state can be effectively blocked because the grid plates 4-1-6 are arranged in an inclined shape, the impact force of the fluid is reduced, the gas phase entrained liquid drops are forced to disperse to the periphery by the blocking action of the grid plates 4-1-6, a larger diffusion angle of materials is realized, the fluid naturally drops under the action of gravity after the kinetic energy is exhausted to form a vertical descending flow state, the liquid phase potential energy is converted into the kinetic energy of a free falling body and falls onto the tray 4-2 of the impact reduction flow equalizing disc, as the overflow holes 4-1-5 are arranged on the descending pipe 4-1-4, namely the material channel is arranged horizontally, and the overflow holes 4-1-5 have a certain height difference from the tray 4-2, the material will thus form a liquid layer with a certain depth on tray 4-2, ensuring that the liquid phase is present in each distributor 4-1 even if tray 4-2 is out of level. Because the number of the distributors 4-1 is large, a certain number of distributors 4-1 can be arranged at any point on the surface of the catalyst bed layer in the reactor to work, so that the uniformity of the distributors 4-1 is guaranteed. Fluid flows into the topmost distribution plate in the reactor from overflow holes 4-1-5 formed in the pipe wall of the material dropping pipe 4-1-3, so that the primary distribution of the materials is realized. Because the materials after passing through the flow reducing and equalizing disc are converted into vertical flow when being distributed on the top distribution disc, and the kinetic energy disappears, the liquid layer on the surface of the top distribution disc tray has no thrust any more, the 'wave pushing' action of the materials on the liquid layer on the distribution disc is eliminated, friendly, stable and uniform inlet conditions are provided for the top distribution disc, and the materials are uniformly distributed on the catalyst bed layer together with the top distribution disc.

When the liquid phase material amount is less, or the upper part of the catalyst bed layer is filled with a protective agent, the hydrogenation reactor provided by the invention is provided with the impact reduction and flow equalization disc, and can replace a top distribution disc in the reactor, so that the integration of impact reduction, flow equalization and distribution is realized.

The following examples are given to illustrate the reaction effect of the present invention, but do not limit the scope of the present invention.

Comparative example 1

A hydrogenation reactor in a coking gasoline hydrofining device of an oil refinery is characterized in that the diameter of the reactor is 3.2m, an upper end enclosure is idle, a top distribution disc is arranged at the inlet of a catalyst bed layer at the uppermost layer, an ERI type bubble cap type gas-liquid distributor which is conventional in the field is used in the top distribution disc, a hydrogenation raw material is coking gasoline fraction, a catalyst is an FGH-21 type hydrofining catalyst produced by the comforting petrochemical research institute, and the process conditions of the reactor are as follows: hydrogen partial pressure of 2.0MPa and volume space velocity of 2.0h^-1The hydrogen-oil volume ratio was 300:1, the reactor inlet temperature was 280 ℃, and the catalyst bed radial temperature and temperature differential are shown in table 1.

Example 1

Compared with comparative example 1, in example 1 of the present invention, the hydrogenation reactor of the present invention was used, the flow reduction and equalization disk of the present invention was disposed in the upper end enclosure of the hydrogenation reactor, and the flow reduction and equalization disk shown in fig. 2 was used in combination with a common ERI type bubble cap gas-liquid distributor. The parameters of the impact reduction flow equalizing disc are as follows: the distance between adjacent grating plates is 100 mm; the inclination angle of the grating plate is 30 degrees; the width of the grating plate is 100 mm; the height of the material dropping pipe is 120 mm; 2 circular overflow holes are horizontally arranged on the pipe wall of the material dropping pipe, and the total sectional area of the overflow holes is 30% of that of the material dropping pipe; the center line of the overflow hole is 50mm away from the upper surface of the tray; the height of the space between the lower surface of the grid and the uppermost edge of the material descending pipe is 50 mm. The tray is assembled by 9 small trays, and each small tray is provided with 2 notched weir type impact reduction flow equalizing discs. The distributors are arranged in a triangular pattern on the tray. The catalyst bed radial temperature and temperature differential are shown in Table 1.

Example 2

The same as example 1, except that the conventional ERI type gas-liquid distributor in the prior art in the original hydrogenation reactor is eliminated, only the flow reducing and equalizing disc arranged in the invention is reserved, and the radial temperature and the temperature difference of the bed layer are shown in the table 1.

TABLE 1 results of application

The embodiments of the present invention have been presented for purposes of illustration and description, and are not intended to be exhaustive or limited to the invention in the form disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art. The embodiment was chosen and described in order to best explain the principles of the invention and the practical application, and to enable others of ordinary skill in the art to understand the invention for various embodiments with various modifications as are suited to the particular use contemplated.

Claims

1. A hydrogenation reactor with a surge-reducing assembly comprises a material inlet pipe, an inlet diffuser, a reactor upper end enclosure, a surge-reducing flow-equalizing disc, a catalyst bed layer, a catalyst support grid, a reactor barrel, a reactor lower end enclosure, an outlet collector, a material outlet pipe and an agent discharging pipe; the device is characterized in that the impact reduction and flow equalization disc is arranged in an idle space of an upper end enclosure of the reactor or at the upper end of a cylinder body of the reactor; the impact reduction and flow equalization plate comprises an impact reduction tray and a plurality of distributors arranged on the impact reduction tray, each distributor comprises a grid, a material descending pipe and a connecting rod, the grids are arranged above the material descending pipes, and the grids are connected with the material descending pipes through the connecting rods; the grating comprises a plurality of grating plates and grating plate connecting rods, and the plurality of grating plates are connected together through the grating plate connecting rods; a plurality of grid plates are arranged in parallel in the horizontal direction and are obliquely arranged, and the oblique direction of the grid plates is towards the outer edge direction of the reactor; a space is formed between the lower surface of the grating plate and the uppermost edge of the material falling pipe, and the space forms a flow channel of gas-phase materials; and the material dropping pipe is provided with an overflow hole.

2. The hydrogenation reactor of claim 1 further comprising a bed unloading pipe, a cold hydrogen tray, an injection tray, and an interbed distribution tray.

3. The hydrogenation reactor of claim 1 wherein said hydrogenation reactor further comprises a top distribution tray.

4. A hydrogenation reactor according to any one of claims 1-3, characterised in that the outermost edges of the de-impaction trays are folded upwards in the setting direction.

5. A hydrogenation reactor according to any one of claims 1 to 3, characterized in that said reduced-lift tray is divided into a plurality of smaller trays, which are assembled to form a unitary tray.

6. A hydrogenation reactor according to any one of claims 1-3, characterized in that the inclination of the grid plate is 10 ° to 90 °.

7. A hydrogenation reactor according to any one of claims 1 to 3, characterized in that the width of the grid plates is 10 to 200mm and the horizontal spacing between adjacent grid plates is 10 to 300 mm.

8. A hydrogenation reactor according to any one of claims 1 to 3, characterized in that the grid formed by a plurality of grid plates arranged in parallel in the horizontal direction is rectangular or cut into a circle.

9. A hydrogenation reactor according to any one of claims 1-3, characterized in that the distributors are arranged in a triangular, quadrangular or circular arrangement on the absorber tray.

10. A hydrogenation reactor according to any of claims 1-3, characterized in that the distributor is fixedly connected to the shock absorbing tray by welding, bolting, screwing or snapping.

11. A hydrogenation reactor according to any one of claims 1 to 3 characterised in that there is a gap between the centreline of the overflow aperture and the upper surface of the de-impaction tray.

12. A hydrogenation reactor according to any one of claims 1-3, characterized in that the height of the space is 5-200 mm.

13. The hydrogenation reactor according to claim 4, wherein the height of the folded edge is 5-80 mm.

14. A hydrogenation reactor according to any one of claims 1 to 3, characterized in that the number of said overflow holes is 1 to 6.

15. A hydrogenation reactor according to any of claims 1-3, characterized in that the total cross-sectional area of the overflow holes is 10-100% of the cross-sectional area of the down-comer pipe.

16. A hydrogenation reactor according to any one of claims 1-3, characterized in that the overflow holes have the shape of a triangle, a quadrangle or a circle.

17. The hydrogenation reactor according to claim 11, wherein the center line of the overflow hole is 5-100 mm from the upper surface of the shock reduction tray.

18. A hydrogenation reactor according to claim 3 wherein the top distribution tray is located below the flow equalization reduction tray and above the uppermost catalyst bed.