A fouling diffuser for an upflow reactor and an upflow reactor

Abstract

A fouling diffuser for an upflow reactor and an upflow reactor, which relate to the field of chemical equipment, include a cylindrical part, an arc-shaped flow guiding part and a conical flow dividing part arranged in sequence from bottom to top. The cylindrical part is a cylindrical structure surrounding the material inlet of the upflow reactor, with a direct flow channel with an open top formed in the middle; the arc-shaped flow guiding part is a cylindrical structure with an arc-shaped side wall and two open ends, and an arc-shaped extension cylinder extending upward is provided at the bottom opening of the arc-shaped flow guiding part; the conical flow dividing part is a conical cylinder structure with a conical top facing downward, and a central flow dividing channel is opened in its center. The present invention can, during the flow dividing process, make the solid particles carried in the material flow be thrown to the area near the reactor side wall due to the centrifugal force and flow along the reflux channel, and then deposit after encountering the fouling area formed by the baffle plate. Finally, while carrying out flow dividing, buffering and uniform distribution of the material flow, the content of solid particles carried therein is effectively reduced.

Description

Technical Field

[0001] The present invention relates to the field of chemical equipment, and specifically to a fouling diffuser for an up-flow reactor and an up-flow reactor. Background Art

[0002] The upgrading and optimization of heavy oil into light oil are important tasks that urgently need to be solved at present. The hydrotreating technology is an effective means to solve the above problems. Through hydrogenation, the effective removal of impurities such as sulfur, nitrogen, metals, resins, and carbon residues in oil products can be achieved, and unsaturated hydrocarbons can be hydrogenated and converted into saturated hydrocarbons. According to the reactor type, the hydrogenation process can be divided into fixed-bed hydrogenation process, suspension-bed hydrogenation process, and ebullated-bed hydrogenation process, among which the fixed-bed hydrogenation process is the most widely used.

[0003] According to the feed direction of the fixed-bed hydrogenation reactor, it can be divided into two forms: up-flow (down-feed) and down-flow (up-feed) fixed-bed hydrogenation reactors. The up-flow fixed-bed reactor has certain advantages in the hydrogenation process of oil products. The up-flow fixed-bed reactor can handle various types of oil products. For example, in inferior oil products such as residue oil and coal liquefied oil, due to the high impurity content, it is easy to cause hydrogenation catalyst poisoning or catalyst pore blockage and rapid deactivation. Moreover, impurities may block the bed layer, causing the pressure drop to increase rapidly, resulting in a deterioration of the reactor operating conditions and even inability to operate normally. If the up-flow hydrogenation reaction process is adopted to make the gas-liquid flow upward in parallel, it can cause the expansion of the catalyst bed layer, increase the void fraction of the bed layer, and avoid the blockage of the catalyst bed layer.

[0004] In current mainstream up-flow reactors, the more representative ones are as follows:

[0005] CN200810117101.1 proposes an up-flow reactor and its application. The up-flow reactor includes an initial distributor at the bottom of the reactor and an intermediate distributor above the initial distributor. The initial distributor consists of a conical baffle plate and a sieve plate located above it; the intermediate distributor consists of an open-hole sieve plate and a sieve plate string structure. The purpose of the up-flow reactor provided by this invention is to achieve uniform gas distribution, thereby improving the utilization rate of the catalyst;

[0006] CN201110353672.7 proposes an up-flow reactor gas-liquid distributor and its application, which includes a distribution tray and a cap-type gas collection and distribution device. The purpose of this invention is to achieve uniform gas phase distribution and improve the mass transfer efficiency of gas-liquid two-phase;

[0007] CN201510697566.9 proposes an up-flow distributor and an up-flow reactor. The purpose of this invention is that through this technical solution, the fluid can be evenly distributed and uniformly mixed after passing through the up-flow distributor;

[0008] The fluidized bed reactor disclosed in US4753721 has a tube ring distributor as the initial distributor at the bottom. Openings are provided at the bottom of the annular tube, and partition plates with slits are arranged on both sides of the tube ring, so that the generated bubbles are broken and redistributed. The intermediate distributor adopts a bubble cap structure, that is, it is connected to the bubble cap above each opening of the perforated plate;

[0009] The initial distributor of US4639354 is a branched tubular distributor. The design of the branched tubular distributor is relatively complex, and a large number of hydrodynamic calculations and experiments are required to ensure the uniform distribution effect of the gas. At the same time, there are certain requirements for the levelness of the installation of the distributor. Therefore, the larger the scale of the reactor, the greater the difficulty of the design of this distributor. The intermediate distributor has two sizes of hole structures. The small holes can only allow the gas phase to pass through, while the large holes mainly pass through the liquid phase. The large holes are connected to the vertical pipe fittings below, and baffle plates are arranged at the bottom of the pipe fittings; the gas-liquid two-phase flow through the intermediate distributor separately and then remix, causing the turbulence of the fluid to achieve uniform distribution; due to the large resistance of the small holes to the flow-through, an air chamber space will be generated in the reactor space below the small holes, reducing the utilization rate of the reactor space, and at the same time, the small holes are easily blocked by impurities, affecting the uniform distribution of the bubbles;

[0010] In addition, Chevron USA Inc. has published two Chinese patents 97193150.X and 00807042.3. Among them, the initial distributor of 00807042.3 is a conical baffle plate, which changes the movement direction of the bubbles entering from the bottom of the reactor, and at the same time serves the purpose of breaking the bubbles to achieve uniform distribution. However, due to the unstable flow of the bubbles, the conical baffle plate cannot effectively avoid the deviation of the bubbles, resulting in uneven expansion of the catalyst bed layer and increased wear of the catalyst particles; in the technology disclosed in 97193150.X, each hole on the perforated plate of the intermediate distributor is connected to the vertical pipe fitting below, and each pipe fitting is laterally provided with a small hole perpendicular to the axial direction of the reactor;

[0011] The above-mentioned upflow reactors and the inlet diffusers inside can only achieve the effects of diffusion and uniform distribution. However, since some of the liquid phase as the reactant may contain solid particles, after entering the upflow reactor, it will block the catalyst bed layer, thereby reducing the reaction efficiency, and in severe cases, even causing the reactor to stop running. Summary of the Invention

[0012] In order to solve the problem that the inlet diffuser used in the existing upflow reactor does not have a slag removal effect, resulting in the blockage of the catalyst bed by solid particles carried in the liquid phase, the present invention provides a fouling diffuser for an upflow reactor and an upflow reactor. During the flow splitting process, the solid particles carried in the logistics can be thrown to the area near the reactor sidewall due to the centrifugal force and flow along the return channel, and then deposit after encountering the fouling area formed by the baffle plate. Finally, while splitting, buffering and distributing the logistics, the content of solid particles carried therein is effectively reduced.

[0013] The technical solution adopted by the present invention to solve the above technical problems is as follows: A fouling diffuser for an upflow reactor includes a cylindrical part, an arc-shaped guiding part and a conical flow splitting part arranged in sequence from bottom to top along the logistics direction. Among them, the cylindrical part is a cylindrical structure surrounding the material inlet of the upflow reactor, and a direct flow channel with an open top is formed in the middle;

[0014] The arc-shaped guiding part is a cylindrical structure with an arc-shaped sidewall and two open ends, and its inner diameter gradually increases from bottom to top. A return channel is formed between the outer sidewall of the arc-shaped guiding part and the inner wall of the upflow reactor. A baffle plate is arranged in the return channel. One end of the baffle plate is in the return channel, and the other end is inclined and fixedly connected to the inner wall of the upflow reactor, so as to form a fouling area with an opening against the logistics direction in the return channel at the connection;

[0015] An arc-shaped extension cylinder extending upward is provided at the bottom opening of the arc-shaped guiding part, and a variable cross-section flow channel with a diameter gradually decreasing first and then increasing from bottom to top is formed in the arc-shaped extension cylinder. A vortex deposition area is formed between the outer wall of the arc-shaped extension cylinder and the inner wall of the arc-shaped guiding part;

[0016] The conical flow splitting part is a conical cylinder structure with a conical top facing downwards, and a central flow splitting channel is opened in the center thereof. A guiding channel is formed between the upper part of the variable cross-section flow channel and the outer sidewall of the conical flow splitting part.

[0017] As an optimized scheme of the above fouling diffuser for an upflow reactor, the centers of the direct flow channel, the variable cross-section flow channel, the central flow splitting channel and the material inlet of the upflow reactor are on the same axis, and the diameter of the central flow splitting channel is smaller than that of the direct flow channel, and the diameter of the narrowest part in the center of the variable cross-section flow channel is not less than that of the direct flow channel.

[0018] As another optimized scheme of the above fouling diffuser for an upflow reactor, the inner diameter of the direct flow channel is 4 - 10 times the diameter of the central flow splitting channel, the diameter of the narrowest part in the center of the variable cross-section flow channel is 1.2 - 1.5 times the inner diameter of the direct flow channel, the diameter of the top of the variable cross-section flow channel is 1.5 - 2 times the inner diameter of the direct flow channel, and the diameter of the bottom of the variable cross-section flow channel is 1.5 - 2 times the inner diameter of the direct flow channel.

[0019] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, the top position of the arc-shaped extension cylinder is lower than the top position of the arc-shaped diversion part, so that part of the material flow in the diversion channel forms a reverse flow to the folding vortex deposition area after being blocked by the inner side wall of the arc-shaped diversion part during the flow along the inner side wall of the upper part of the arc-shaped extension cylinder; the bottom diameter of the arc-shaped extension cylinder is larger than the diameter of the cylindrical part, so that the material flow in the return channel is blocked by the outer side of the cylindrical part and then converges into the variable cross-section flow channel along the inner side wall of the lower part of the arc-shaped extension cylinder.

[0020] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, the height of the arc-shaped extension cylinder is 30-60% of the height of the arc-shaped diversion part, and the height of the cylindrical part is 20-30% of the height of the arc-shaped diversion part.

[0021] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, the distance between the arc-shaped extension cylinder and the cylindrical part is 40-60% of the width of the return channel.

[0022] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, the top diameter of the conical shunt part is larger than the top diameter of the arc-shaped extension cylinder, and the height of the top of the arc-shaped diversion part is between the bottom end and the top end of the conical shunt part.

[0023] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, the top diameter of the conical shunt part is 1.2-1.5 times the top diameter of the arc-shaped extension cylinder, and the height of the top of the arc-shaped diversion part is at the upper position of the side wall of the conical shunt part.

[0024] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, there are two groups of baffle plates in the return channel, and they are arranged in sequence along the material flow direction. The top position of the first group of baffle plates is higher than the bottom position of the arc-shaped diversion part.

[0025] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, the width of the return channel gradually becomes narrower from top to bottom.

[0026] As another optimized solution for the fouling diffuser of the above-mentioned upflow reactor, the cylindrical part is located inside the upflow reactor to form a baffle for guiding the change of the material flow direction in the return channel.

[0027] An upflow reactor is provided with a diffuser between the bottom material inlet and the distribution plate of the reactor, and the diffuser is the above-mentioned fouling diffuser.

[0028] Compared with the prior art, the present invention has the following beneficial effects:

[0029] 1) The fouling diffuser of the present invention is divided into a three-stage structure, which is successively a cylindrical part, an arc-shaped flow guiding part, and a conical flow dividing part from bottom to top. At the bottom opening of the arc-shaped flow guiding part, there is an arc-shaped extension cylinder extending upward, thus forming a main flow channel composed of a straight flow channel, a variable flow channel, and a central flow dividing channel. At the same time, a flow guiding channel is formed between the arc-shaped extension cylinder and the conical flow dividing part, and a reflux channel is formed between the arc-shaped flow guiding part and the inner wall of the reactor. The cooperation of the reflux channel and the flow guiding channel realizes the flow division while deflecting part of the material flow 180° for reflux, and then merging into the main flow channel after reflux, realizing the circulation and uniform distribution at the bottom of the reactor. During the reflux process, the solid particles carried in the material flow are thrown to the area near the side wall of the reactor due to the centrifugal force and flow along the reflux channel, and then deposit after encountering the fouling area formed by the baffle plate. Finally, while dividing, buffering, and uniformly distributing the material flow, the content of solid particles carried therein is effectively reduced;

[0030] 2) A vortex deposition area is formed by the cooperation between the arc-shaped flow guiding part and the arc-shaped extension cylinder of the present invention. The existence of the vortex deposition area can not only divide and slow down the material flow in the flow guiding channel, but also enable the solid particles carried therein to settle in the vortex deposition area;

[0031] 3) The fouling diffuser of the present invention can not only effectively slow down and uniformly distribute the liquid material flow entering the up-flow reactor, but more importantly, can effectively reduce the content of solid particles in the liquid material flow of the up-flow reactor, prevent these solid particles from blocking the catalyst bed layer after entering the catalyst bed layer, and reduce the reaction efficiency. Brief Description of the Drawings

[0032] Figure 1 is a schematic structural diagram of the present invention;

[0033] Reference numerals: 1, cylindrical part; 101, straight flow channel; 2, arc-shaped flow guiding part; 201, arc-shaped extension cylinder; 202, variable flow channel; 203, vortex deposition area; 3, conical flow dividing part; 301, central flow dividing channel; 4, flow guiding channel; 5, reflux channel; 501, baffle plate; 502, fouling area. Detailed Embodiments

[0034] The technical solutions of the present invention will be further elaborated in detail below in combination with specific embodiments. For parts not clarified in the following embodiments of the present invention, such as other structures inside the up-flow reactor (technologies related to the catalyst bed layer, structure of the distributor), etc., are regarded as the prior art known or should be known to those skilled in the art.

[0035] Embodiment 1

[0036] A fouling diffuser for an up-flow reactor, the fouling diffuser is a split structure and consists of three parts, asFigure 1 As shown, it includes a cylindrical part 1, an arc-shaped flow guiding part 2, and a conical flow dividing part 3 arranged in sequence from bottom to top along the material flow direction in the up-flow reactor. Among them, the cylindrical part 1 is a cylindrical structure arranged around the material inlet of the up-flow reactor. Both ends of the cylinder are open. The bottom opening is connected to the material inlet, and a straight channel 101 with an open top is formed in the middle. In practice, the bottom of the cylinder is generally welded to the bottom of the up-flow reactor, and it surrounds the material inlet, and its central axis coincides with the central axis of the reactor;

[0037] The arc-shaped flow guiding part 2 is a cylindrical structure with an arc-shaped side wall and open ends at both ends, and its inner diameter gradually increases from bottom to top. That is to say, the arc-shaped flow guiding part 2 is a frustum-shaped structure with open ends at the top and bottom and a hollow interior, and its side wall is an arc convex away from the center of the reactor. The open ends at the top and bottom form a passage for the material to pass through. In practice, several connecting legs are arranged around the outer side wall of the arc-shaped flow guiding part 2. The bottom ends of these connecting legs can be vertically fixed on the bottom wall of the up-flow reactor or inclinedly fixed on the bottom wall of the up-flow reactor. Of course, they can also be fixed to the bottom surface of the upper distribution plate above in a vertical or inclined manner, so as to realize the fixed installation of the arc-shaped flow guiding part 2. A reflux channel 5 is formed between the outer side wall of the arc-shaped flow guiding part 2 and the inner wall of the up-flow reactor. The reflux channel 5 is annular. There is a certain distance between the top of the arc-shaped flow guiding part 2 and the distribution plate inside the up-flow reactor. This distance is connected to the reflux channel 5, so that some materials that have not entered the distributor will turn back 180° when passing through. A baffle 501 is arranged in the reflux channel 5. In practice, the structure of the baffle 501 generally has two types. One is a cylindrical body with open ends at both ends of a frustum shape, whose central axis is coaxial with the cylindrical part 1 and surrounds the cylindrical part 1. The bottom end is fixedly connected to the inner wall of the bottom of the up-flow reactor, and the inner diameter gradually increases from bottom to top, so that its side wall forms an inclined plane with a certain acute angle with the inner wall of the bottom of the up-flow reactor, and the formed acute angle is the fouling area 502. Another structure is that the baffle 501 is several plate-shaped members distributed along the outer side wall of the reflux channel 5, that is, the inner side wall of the lower part of the up-flow reactor. These plate-shaped members are inclined and not connected to each other to form a channel. The top ends are in the reflux channel 5, and the bottom ends are fixed on the inner side wall of the lower part of the up-flow reactor. The width direction of the plate-shaped members forms a certain acute angle with the inner side wall of the reactor, which is the fouling area 502. These plate-shaped members can be at the same height or different heights inside the reactor. One end of the baffle 501 is in the reflux channel 5, and the other end is inclinedly fixedly connected to the inner wall of the up-flow reactor. In practice, when the baffle 501 is a frustum-shaped cylindrical body, the top end of the cylindrical body is in the reflux channel 5, and the bottom end is fixed on the bottom wall of the up-flow reactor. When the baffle 501 is a plate-shaped member with a certain width, the top end of the plate-shaped member is in the reflux channel 5, and the bottom end is fixed on the bottom wall of the up-flow reactor, so as to form a fouling area 502 with the opening facing against the flow direction of the material in the reflux channel 5 at the connection. Due to the existence of the reflux channel 5, the flow direction of the material flow turns 180°. During this process, the solid particles carried by the material flow will be thrown to the position close to the inner wall of the lower part of the reactor and flow along the reflux channel 5 due to the centrifugal force, and then be blocked by the baffle 501, and the speed will decrease and deposit in the fouling area 502;

[0038] An arc-shaped extension cylinder 201 extends upward from the bottom opening of the arc-shaped guiding part 2. In practice, the arc-shaped guiding part 2 and the arc-shaped extension cylinder 201 are of an integral structure, and a variable flow channel 202 with a diameter gradually decreasing from bottom to top and then gradually increasing is formed inside the arc-shaped extension cylinder 201. A vortex deposition area 203 is formed between the outer wall of the arc-shaped extension cylinder 201 and the inner wall of the arc-shaped guiding part 2. Part of the material flow passing through the variable flow channel 202 inside the arc-shaped extension cylinder 201 will change its flow direction due to the obstruction of the upper region of the arc-shaped guiding part 2 and flow towards the arc-shaped cavity with an opening formed by the outer wall of the arc-shaped extension cylinder 201 and the inner wall of the lower region of the arc-shaped guiding part 2. After hitting the inner wall of the arc-shaped cavity, it flows out along the outer side wall of the arc-shaped extension cylinder 201. During the entire flow process, the solid particles carried therein will be thrown onto the inner wall of the vortex deposition area 203 due to the centrifugal force and then deposit;

[0039] The conical shunt part 3 is a conical cylinder structure with the conical top facing downwards, that is, its large-diameter opening end faces upwards, and there is a certain distance between its top and the distribution plate. There are generally three fixing methods for the conical shunt part 3. One is to fix it on the lower surface of the distribution plate through legs, another is to fix it on the inner wall of the arc-shaped guiding part 2 through legs, and the third is to fix it on the inner wall of the reactor through legs. These three fixing methods can be used alternatively or in combination. And a central shunt channel 301 is opened in its center. In practice, the central shunt channel 301 is a through hole. A guiding channel 4 is formed between the upper part of the variable flow channel 202 and the outer side wall of the conical shunt part 3. The guiding channel 4 and the reflux channel 5 are connected and matched, thereby realizing the 180° turning flow of the material flow.

[0040] The above is the basic implementation mode of the present invention. Further improvements, optimizations and limitations can be made on this basis to obtain the following embodiments:

[0041] Embodiment 2

[0042] This embodiment further limits the main flow channel on the basis of Embodiment 1. Its main structure is the same as that of Embodiment 1. The improvement lies in: as Figure 1 shown, the centers of the straight flow channel 101, the variable flow channel 202, the central shunt channel 301 and the material inlet of the up-flow reactor are on the same axis, and the diameter of the central shunt channel 301 is smaller than the diameter of the straight flow channel 101, and the diameter of the narrowest part at the center of the variable flow channel 202 is not less than the diameter of the straight flow channel 101;

[0043] In this embodiment, the inner diameter of the straight channel 101 is 4 - 10 times the diameter of the central shunt channel 301. The diameter at the narrowest part in the center of the variable - flow channel 202 is 1.2 - 1.5 times the inner diameter of the straight channel 101. The diameter at the top end of the variable - flow channel 202 is 1.5 - 2 times the inner diameter of the straight channel 101. The diameter at the bottom end of the variable - flow channel 202 is 1.5 - 2 times the inner diameter of the straight channel 101.

[0044] Embodiment 3

[0045] This embodiment further defines the arc - shaped extension cylinder 201 on the basis of Embodiment 1. Its main structure is the same as that of Embodiment 1. The improvement lies in that, as Figure 1 shown, the position of the top end of the arc - shaped extension cylinder 201 is lower than the position of the top end of the arc - shaped guide part 2. Thus, when part of the material flow in the guide channel 4 flows along the inner side wall of the upper part of the arc - shaped extension cylinder 201 and is blocked by the inner side wall of the arc - shaped guide part 2, a reverse flow in the folding - vortex deposition area 203 is formed. The diameter of the bottom end of the arc - shaped extension cylinder 201 is larger than the diameter of the cylinder part 1. Thus, when the material flow in the return channel 5 is blocked by the outside of the cylinder part 1, it converges into the variable - flow channel 202 along the inner side wall of the lower part of the arc - shaped extension cylinder 201;

[0046] In this embodiment, the height of the arc - shaped extension cylinder 201 is 30 - 60% of the height of the arc - shaped guide part 2, and the height of the cylinder part 1 is 20 - 30% of the height of the arc - shaped guide part 2;

[0047] In this embodiment, the distance between the arc - shaped extension cylinder 201 and the cylinder part 1 is 40 - 60% of the width of the return channel 5.

[0048] Embodiment 4

[0049] This embodiment further defines the conical shunt part 3 on the basis of Embodiment 1. Its main structure is the same as that of Embodiment 1. The improvement lies in that, as Figure 1 shown, the top - end diameter of the conical shunt part 3 is larger than the top - end diameter of the arc - shaped extension cylinder 201, and the height of the top end of the arc - shaped guide part 2 is between the bottom end and the top end of the conical shunt part 3;

[0050] In this embodiment, the top - end diameter of the conical shunt part 3 is 1.2 - 1.5 times the top - end diameter of the arc - shaped extension cylinder 201, and the height of the top end of the arc - shaped guide part 2 is at the upper part of the side wall of the conical shunt part 3. Generally, this upper part refers to the area of 60 - 80% of its height.

[0051] Embodiment 5

[0052] This embodiment further defines the return channel 5 on the basis of Embodiment 1. Its main structure is the same as that of Embodiment 1. The improvement lies in that, as Figure 1As shown, there are two groups of baffle plates 501 provided in the reflux channel 5, and they are arranged in sequence along the material flow direction. The top position of the first group of baffle plates 501 is higher than the bottom position of the arc-shaped diversion part 2. Compared with the top end of the first group of baffle plates 501, the top end of the second group of baffle plates 501 is closer to the outer side wall of the arc-shaped diversion part 2. The included angle formed by the baffle plates 501 is generally 30-60°, and the position where its top end is located is 30-50% of the width of the reflux channel 5;

[0053] In this embodiment, the width of the reflux channel 5 gradually narrows from top to bottom. In practice, the lower part of the upflow reactor is generally hemispherical, and a material inlet is provided at its lowest point. At this time, a reflux channel 5 is formed between the outer side wall of the arc-shaped diversion part 2 and the inner side wall of the hemispherical shape. And, according to the actual situation, the arc angle of the arc-shaped diversion part 2 is adjusted, so that the width of the reflux channel 5 gradually narrows from top to bottom.

[0054] Embodiment 6

[0055] This embodiment is a further limitation on the cylindrical part 1 on the basis of Embodiment 1. Its main structure is the same as that of Embodiment 1. The improvement lies in: as Figure 1 shown, the cylindrical part 1 is located inside the upflow reactor and forms a baffle member for guiding the flow direction change of the material in the reflux channel 5. That is, the existence of the cylindrical part 1 can block and guide the material in the reflux channel 5 to change direction, so that it can better flow into the variable flow channel 202, and it can also play a certain sedimentation role, so that some solid particles are deposited at this position.

[0056] Embodiment 7

[0057] An upflow reactor is provided with a diffuser between the bottom material inlet of the reactor and the distribution plate, and the diffuser is the above-mentioned fouling diffuser.

Claims

1. A fouling diffuser for an upflow reactor, characterized in that: It includes a cylindrical part (1), an arc-shaped flow guiding part (2) and a conical flow dividing part (3) which are arranged successively from bottom to top along the logistics direction. Among them, the cylindrical part (1) is a cylindrical structure surrounding the material inlet of the up-flow reactor, and a straight flow channel (101) with an open top is formed in the middle; The arc-shaped flow guiding part (2) is a cylindrical structure with an arc-shaped side wall and two open ends, and its inner diameter gradually increases from bottom to top. A reflux channel (5) is formed between the outer side wall of the arc-shaped flow guiding part (2) and the inner wall of the up-flow reactor. A baffle plate (501) is arranged in the reflux channel (5). One end of the baffle plate (501) is in the reflux channel (5), and the other end is fixedly connected to the inner wall of the up-flow reactor obliquely, so as to form a fouling accumulation area (502) with an opening against the logistics direction in the reflux channel (5); An arc-shaped extension cylinder (201) extending upward is provided at the bottom opening of the arc-shaped flow guiding part (2), and a variable cross-section flow channel (202) with a diameter gradually decreasing first and then increasing from bottom to top is formed in the arc-shaped extension cylinder (201). An eddy current deposition area (203) is formed between the outer wall of the arc-shaped extension cylinder (201) and the inner wall of the arc-shaped flow guiding part (2); The conical flow dividing part (3) is a conical cylinder structure with a conical top facing downwards, and a central flow dividing channel (301) is opened in its center. A flow guiding channel (4) is formed between the upper part of the variable cross-section flow channel (202) and the outer side wall of the conical flow dividing part (3).

2. The fouling diffuser for an upflow reactor according to claim 1, characterized in that: The centers of the straight flow channel (101), the variable cross-section flow channel (202), the central flow dividing channel (301) and the material inlet of the up-flow reactor are on the same axis. The diameter of the central flow dividing channel (301) is smaller than that of the straight flow channel (101), and the diameter of the narrowest part in the center of the variable cross-section flow channel (202) is not less than that of the straight flow channel (101).

3. The fouling diffuser for an upflow reactor according to claim 2, characterized in that: The inner diameter of the straight flow channel (101) is 4-10 times the diameter of the central flow dividing channel (301). The diameter of the narrowest part in the center of the variable cross-section flow channel (202) is 1.2-1.5 times the inner diameter of the straight flow channel (101). The diameter of the top of the variable cross-section flow channel (202) is 1.5-2 times the inner diameter of the straight flow channel (101). The diameter of the bottom of the variable cross-section flow channel (202) is 1.5-2 times the inner diameter of the straight flow channel (101).

4. The fouling diffuser for an upflow reactor according to claim 1, wherein: The position of the top of the arc-shaped extension cylinder (201) is lower than the position of the top of the arc-shaped flow guiding part (2), so that part of the logistics in the flow guiding channel (4) forms a reverse flow towards the eddy current deposition area (203) after being blocked by the inner side wall of the arc-shaped flow guiding part (2) during the flow along the inner side wall of the upper part of the arc-shaped extension cylinder (201). The bottom diameter of the arc-shaped extension cylinder (201) is larger than the diameter of the cylindrical part (1), so that the logistics in the reflux channel (5) is blocked by the outer side of the cylindrical part (1) and then converges into the variable cross-section flow channel (202) along the inner side wall of the lower part of the arc-shaped extension cylinder (201).

5. The fouling diffuser for an upflow reactor according to claim 4, wherein: The height of the arc-shaped extension cylinder (201) is 30-60% of the height of the arc-shaped flow guiding part (2). The height of the cylindrical part (l) is 20-30% of the height of the arc-shaped flow guiding part (2).

6. The fouling diffuser for an upflow reactor according to claim 4, characterized in that: The distance between the arc-shaped extension cylinder (201) and the cylindrical part (1) is 40-60% of the width of the reflux channel (5).

7. The fouling diffuser for an upflow reactor according to claim 1, characterized in that: The top diameter of the conical diversion part (3) is larger than the top diameter of the arc-shaped extension cylinder (201), and the height of the top of the arc-shaped diversion part (2) is between the bottom end and the top end of the conical diversion part (3).

8. A fouling diffuser for an upflow reactor according to claim 7, characterized in that: The top diameter of the conical diversion part (3) is 1.2-1.5 times the top diameter of the arc-shaped extension cylinder (201), and the height of the top of the arc-shaped diversion part (2) is at the upper position of the side wall of the conical diversion part (3).

9. A fouling diffuser for an upflow reactor according to claim 1, characterized in that: There are two groups of baffle plates (501) arranged in the reflux channel (5) in sequence along the material flow direction. The top position of the first group of baffle plates (501) is higher than the bottom end position of the arc-shaped diversion part (2).

10. A fouling diffuser for an upflow reactor according to claim 1, characterized in that: The width of the reflux channel (5) gradually becomes narrower from top to bottom.

11. A fouling diffuser for an upflow reactor according to claim 1, wherein: The cylindrical part (1) is located in the up-flow reactor and forms a baffle member for guiding the change of direction of the material flow in the reflux channel (5).

12. An upflow reactor is provided with a diffuser between the bottom material inlet of the reactor and the distribution plate, and is characterized in that: The diffuser is the fouling diffuser according to any one of claims 1-11.

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