Fixed ball type gas-liquid flow stabilizing disc and upflow type reactor

Abstract

The application discloses a fixed ball type gas-liquid flow stabilizing disc and an upflow type reactor, and belongs to the field of chemical equipment. The fixed ball type gas-liquid flow stabilizing disc comprises spherical bodies filled in a containing cavity, and passages for passing gas-liquid mixture are arranged on opposite two side walls of the containing cavity. The surface of the spherical bodies is distributed with a plurality of protrusions, and the protrusions form gaps between two adjacent spherical bodies for buffering the gas-liquid mixture. The fixed ball type gas-liquid flow stabilizing disc is filled with the spherical bodies with protrusions on the surface in the containing cavity, the spherical bodies are pressed and fixed with each other, and the gaps for buffering the gas-liquid mixture are formed between the spherical bodies. The gaps are communicated with each other, and the baffling passages similar to a labyrinth form are formed for guiding the flow of the gas-liquid mixture. The fixed ball type gas-liquid flow stabilizing disc can effectively reduce the impact of the gas-liquid on the spherical bodies, reduce the flow rate of the gas-liquid mixture, and the pressure drop of the gas-liquid mixture after passing through the flow stabilizing disc is small, so that the gas-liquid separation can be effectively promoted.

Description

Technical Field

[0001] This invention relates to the field of chemical equipment, specifically a fixed spherical gas-liquid stabilizing plate and an upflow reactor. Background Technology

[0002] The market demand for clean oil products is increasing rapidly. Therefore, the upgrading and improvement of heavy oils to lighter and higher quality are urgent tasks. Hydrotreating technology is an effective means to address these issues. Hydrotreating can effectively remove impurities such as sulfur, nitrogen, metals, gums, and residual carbon from oil products, and can also convert unsaturated hydrocarbons into saturated hydrocarbons. Based on reactor type, hydrotreating processes can be classified into fixed-bed hydrotreating, suspended-bed hydrotreating, and fluidized-bed hydrotreating, with fixed-bed hydrotreating being the most widely used.

[0003] Based on the feed direction, fixed-bed hydrotreating reactors can be divided into two types: upflow (bottom feed) and downflow (top feed). Upflow fixed-bed reactors offer certain advantages in oil hydrotreating. They can process various types of oils, such as low-quality residue oil and coal liquefaction oil. Due to high impurity content, these oils are prone to catalyst poisoning or pore blockage, leading to rapid deactivation. Furthermore, impurities can clog the bed, causing a rapid increase in pressure drop and deteriorating reactor conditions, even rendering them unusable. Upflow hydrotreating, with its upward co-current flow of gas and liquid, expands the catalyst bed, increasing its porosity and preventing blockage.

[0004] Among the mainstream upflow reactors currently available, some representative examples include:

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

[0006] CN201110353672.7 proposes a gas-liquid distributor for an upflow reactor and its application, comprising a distribution tray and a cap-type gas collector and distributor. The purpose of this invention is to achieve uniform distribution of the gas phase and improve the mass transfer efficiency between the gas and liquid phases.

[0007] CN201510697566.9 proposes an upflow distributor and an upflow reactor. The purpose of this invention is to enable the fluid to be uniformly distributed and mixed after passing through the upflow distributor.

[0008] US4753721 discloses a fluidized bed reactor, with a bottom initial distributor being a tube ring distributor. The tube ring has openings at the bottom and slit baffles on both sides to break up and redistribute the generated bubbles. The intermediate distributor adopts a bubble cap structure, that is, a bubble cap is connected above each opening of the porous plate.

[0009] The initial distributor in US4639354 is a branched tubular distributor. The design of branched tubular distributors is relatively complex, requiring extensive fluid dynamics calculations and experiments to ensure uniform gas distribution. Furthermore, the horizontal alignment of the distributor installation is critical; therefore, the larger the reactor, the more difficult the distributor design becomes. The intermediate distributor has two orifice sizes: small orifices allow only the gas phase to pass through, while large orifices primarily allow the liquid phase. The large orifices are connected to a vertical pipe with baffles at the bottom. The gas and liquid phases are separated and remixed through the intermediate distributor, creating turbulence to achieve uniform distribution. Due to the high resistance at the small orifices, a gas chamber is created below the orifice, reducing reactor space utilization. Additionally, the small orifices are easily clogged by impurities, affecting bubble uniformity.

[0010] In addition, Chevron USA has published two Chinese patents, 97193150.X and 00807042.3. In the initial distributor of 00807042.3, a conical baffle is used to change the direction of movement of bubbles entering from the bottom of the reactor, and at the same time, it breaks the bubbles to achieve uniform distribution. However, since the flow of bubbles is unstable, the conical baffle cannot effectively prevent the bubbles from deflecting, resulting in uneven expansion of the catalyst bed and increased wear of catalyst particles. In the technology disclosed in 97193150.X, the intermediate distributor is designed with each hole on a porous plate connected to a vertical pipe below, and each pipe has a small hole on its side perpendicular to the reactor axis.

[0011] A comprehensive analysis of the basic characteristics of upflow reactors reveals some common problems:

[0012] (1) When the reactor diameter is large, an inlet diffuser and a distributor are needed to distribute the reactants evenly.

[0013] (2) The upper part of the reactor lacks internal components for stabilizing the bed or for initial gas-liquid separation. Summary of the Invention

[0014] The purpose of this invention is to provide a fixed spherical gas-liquid stabilizing plate and an upflow reactor. By filling the containment cavity with spherical bodies having protrusions on their surfaces, the spherical bodies are pressed and fixed together, forming gaps that buffer the gas-liquid mixture. These gaps are interconnected, forming a labyrinth-like flow channel that guides the gas-liquid mixture. This not only effectively reduces the impact of gas and liquid on the spherical bodies and lowers the flow velocity of the gas-liquid mixture, but also results in a very small pressure drop after the gas-liquid mixture flows through the stabilizing plate, which can effectively promote gas-liquid separation.

[0015] The technical solution adopted by the present invention to achieve the above-mentioned technical objective is as follows: a fixed spherical gas-liquid stabilizing disk, comprising a spherical body filled in a receiving cavity, having channels for gas-liquid mixture to pass through on two opposite side walls of the receiving cavity, and having a plurality of protrusions distributed on the surface of the spherical body, which form a gap for buffering the gas-liquid mixture between two adjacent spherical bodies.

[0016] As an optimized solution for the aforementioned fixed spherical gas-liquid stabilizing plate, the height of the protrusion is 20-50% of the diameter of the sphere.

[0017] As another optimized solution for the above-mentioned fixed spherical gas-liquid stabilizing plate, the sphere is a solid sphere with a diameter of 5-20mm and a gap of 1-5mm between two adjacent spheres.

[0018] As another optimized solution for the aforementioned fixed spherical gas-liquid stabilizing disk, the accommodating cavity is a chamber formed by the cooperation of an upper grid plate, a lower grid plate, and the inner wall of an upflow reactor.

[0019] As another optimized solution for the aforementioned fixed spherical gas-liquid stabilizing plate, the receiving cavity has a gas-liquid separation cylinder on the downstream side along the flow direction of the gas-liquid mixture. An overflow channel for the gas-liquid mixture is formed between the side wall of the gas-liquid separation cylinder and the edge of the receiving cavity. The gas-liquid mixture flows into the gas-liquid separation cylinder from the top opening through the overflow channel. The liquid phase is discharged from the liquid phase discharge pipe provided in the upper part of the side wall of the gas-liquid separation cylinder, and the gas phase is discharged from the top opening of the gas-liquid separation cylinder.

[0020] An upflow reactor has a flow stabilizer plate in the upper region of the reactor, and the channel through which the gas and liquid phases pass is aligned with the material flow direction within the upflow reactor.

[0021] As an optimized solution for the above-mentioned upflow reactor, the upflow reactor has a gas-liquid mixture inlet at the bottom, and a scale-collecting inlet diffuser is provided above the gas-liquid mixture inlet, including a cylindrical part, an arc-shaped guide part and a conical diverter part arranged sequentially from bottom to top along the material flow direction. The cylindrical part is a cylindrical structure arranged around the material inlet of the upflow reactor, forming a direct flow channel with an open top in the middle.

[0022] The arc-shaped flow guide is a cylindrical structure with arc-shaped sidewalls and open ends, and its inner diameter gradually increases from bottom to top. A reflux channel is formed between the outer sidewall of the arc-shaped flow guide and the inner wall of the upflow reactor. A baffle is provided in the reflux channel. One end of the baffle is in the reflux channel, and the other end is inclined and fixedly connected to the inner wall of the upflow reactor, thereby forming a scale collection area with an opening opposite to the flow direction in the reflux channel at the connection.

[0023] The arc-shaped guide section has an upwardly extending arc-shaped extension cylinder at the bottom opening, and a variable diameter flow channel is formed inside the arc-shaped extension cylinder, with the diameter gradually decreasing from bottom to top and then gradually increasing. A vortex deposition zone is formed between the outer wall of the arc-shaped extension cylinder and the inner wall of the arc-shaped guide section.

[0024] The conical diversion section is a conical cylinder structure with the top of the cone facing downwards, and a central diversion channel is opened in the center of it. A guide channel is formed between the upper part of the variable diameter flow channel and the outer wall of the conical diversion section.

[0025] As another optimization scheme for the above-mentioned upflow reactor, the center of the direct flow channel, the variable diameter flow channel, the central diversion channel and the material inlet of the upflow reactor are on the same axis, and the diameter of the central diversion channel is smaller than the diameter of the direct flow channel, and the diameter of the narrowest point of the variable diameter flow channel is not smaller than the diameter of the direct flow channel.

[0026] As another optimization scheme for the above-mentioned upflow reactor, the top of the arc-shaped extension cylinder is lower than the top of the arc-shaped guide section, so that some of the material in the guide channel is blocked by the inner wall of the arc-shaped guide section during its flow along the upper inner wall of the arc-shaped extension cylinder, forming a backflow that turns towards the eddy deposition zone; the bottom diameter of the arc-shaped extension cylinder is larger than the diameter of the cylindrical section, so that the material in the return channel is blocked by the outer side of the cylindrical section and flows into the variable diameter channel along the lower inner wall of the arc-shaped extension cylinder.

[0027] As another optimization scheme for the above-mentioned upflow reactor, the top diameter of the conical diversion section is larger than the top diameter of the arc-shaped extension tube, and the height of the top of the arc-shaped guide section is between the bottom and top of the conical diversion section.

[0028] As another optimization scheme for the above-mentioned upflow reactor, the baffles in the return channel are in two sets and are arranged sequentially along the flow direction of the material. The top of the first set of baffles is higher than the bottom of the arc-shaped guide section.

[0029] As another optimization scheme for the above-mentioned upflow reactor, the width of the reflux channel gradually narrows from top to bottom.

[0030] As another optimized solution for the aforementioned upflow reactor, the cylindrical section is located inside the upflow reactor, forming a flow-blocking component that guides the flow direction change within the return channel.

[0031] Compared with the prior art, the present invention has the following beneficial effects:

[0032] 1) The flow stabilizing plate of the present invention has spherical bodies with protrusions on the surface of the cavity. The spherical bodies are pressed and fixed together and form gaps that buffer the gas-liquid mixture. These gaps are interconnected and form a labyrinth-like flow channel for guiding the gas-liquid mixture. This not only effectively reduces the impact of gas and liquid on the spherical bodies and reduces the flow rate of the gas-liquid mixture, but also results in a small pressure drop after the gas-liquid mixture flows through the flow stabilizing plate, which can effectively promote gas-liquid separation.

[0033] 2) The scale-collecting inlet diffuser in the upflow reactor of this invention has a three-section structure, consisting of a cylindrical section, an arc-shaped guide section, and a conical diversion section from bottom to top. The arc-shaped guide section has an upward-extending arc-shaped extension cylinder at its bottom opening, thus forming a main channel consisting of a direct flow channel, a variable diameter flow channel, and a central diversion channel. At the same time, a guide channel is formed between the arc-shaped extension cylinder and the conical diversion section, and a return channel is formed between the arc-shaped guide section and the inner wall of the reactor. The cooperation between the return channel and the guide channel achieves both diversion and 180° deflection of part of the material back to the main channel, achieving circulation and uniform distribution at the bottom of the reactor. During the return process, the solid particles carried in the material are thrown to the area near the side wall of the reactor by centrifugal force and flow along the return channel. They then encounter the scale-collecting area formed by the baffle plate and are deposited. Ultimately, the material is effectively reduced in terms of solid particle content while being diverted, buffered, and uniformly distributed.

[0034] 3) The arc-shaped guide section and the arc-shaped extension cylinder of the scale-collecting inlet diffuser of the present invention form a vortex deposition zone. The existence of the vortex deposition zone can divert and slow down the flow of material in the guide channel, and also cause the solid particles carried therein to settle in the vortex deposition zone.

[0035] 4) The scale-collecting inlet diffuser of the present invention can not only effectively slow down and distribute the liquid stream entering the upflow reactor, but more importantly, it can effectively reduce the content of solid particles in the liquid stream of the upflow reactor, preventing these solid particles from entering the catalyst bed and clogging the bed, thus reducing the reaction efficiency. Attached Figure Description

[0036] Figure 1 This is a schematic diagram of the fixed gas-liquid flow stabilizing disk in this invention;

[0037] Figure 2 This is a schematic diagram of the overall structure of the upflow reactor in this invention;

[0038] Figure 3This is a schematic diagram of the scale-collecting inlet diffuser in this invention;

[0039] Reference numerals: 1. Stabilizing plate; 101. Receiving cavity; 102. Spherical body; 103. Upper grid plate; 104. Lower grid plate; 2. Gas-liquid separation cylinder; 201. Overflow channel; 202. Liquid phase discharge pipe; 3. Cylindrical section; 301. Straight channel; 4. Arc-shaped guide section; 401. Arc-shaped extension cylinder; 402. Variable diameter flow channel; 403. Vortex deposition zone; 5. Conical diversion section; 501. Central diversion channel; 6. Guide channel; 7. Return channel; 701. Baffle plate; 702. Scale collection zone. Detailed Implementation

[0040] The technical solution of the present invention will be further described in detail below with reference to specific embodiments. Parts not explained in the following embodiments of the present invention, such as other structures inside the upflow reactor (catalyst bed related technology, distributor structure, etc.), are all considered to be prior art known or should be known by those skilled in the art.

[0041] Example 1

[0042] A fixed spherical gas-liquid stabilizing plate, such as Figure 1 As shown, the cavity includes spherical bodies 102 filled within the receiving cavity 101, with the spherical bodies 102 pressing against each other to fix them within the cavity 101. The spherical bodies 102 can be solid or hollow, spherical or elliptical, and are made of a material that does not react with the liquid phase. The receiving cavity 101 has two opposite sidewalls with channels for the gas-liquid mixture to pass through. These channels can be narrow slits or holes. Whether slits or holes, their dimensions are such that the spherical bodies 102 cannot pass through them. Preferably, the two opposite sidewalls... The channels on the sidewalls are one-to-one, although they can also be non-corresponding. The surface of the sphere 102 has several protrusions, which are generally cylindrical, conical, or other shapes. The number of protrusions is generally evenly distributed on the surface of the sphere, and there is a gap between any protrusion and its adjacent protrusion. The gap, the height and diameter of the protrusion can be set according to the actual situation. These protrusions form gaps between two adjacent spheres 102 to buffer the gas-liquid mixture. These gaps are interconnected to form a maze-like flow channel for guiding the gas-liquid mixture.

[0043] In this embodiment, the height of the protrusions on the surface of the sphere 102 is 20-50% of the diameter of the sphere 102, and the height of the protrusions on the surface of the same sphere 102 can be the same or different.

[0044] In this embodiment, the sphere 102 is a solid sphere with a diameter of 5-20 mm. When these spheres 102 are pressed together and fixed in the receiving cavity 101, the gap between two adjacent spheres 102 is 1-5 mm.

[0045] In this embodiment, the receiving cavity 101 is a chamber formed by the cooperation of the upper grid plate 103, the lower grid plate 104 and the inner wall of the upper flow reactor;

[0046] In this embodiment, the receiving cavity 101 is a chamber with thickness or height, and its horizontal dimension is generally matched with the internal dimensions of the upflow reactor, so that it can be installed horizontally inside the upflow reactor. At this time, the channels for gas and liquid phases to pass through are distributed on the upper and lower surfaces in the thickness or height direction. The receiving cavity 101 can be made into a closed box, and the horizontal direction of the box matches the inner wall of the upflow reactor, so that it is fixed inside the upflow reactor. At this time, channels for gas and liquid phases to pass through are provided on the upper and lower surfaces. Of course, a chamber can also be formed by the cooperation of the upper grid plate 103, the lower grid plate 104 and the inner wall of the upflow reactor. In this case, the edges of the upper grid plate 103 and the lower grid plate 104 are fixed to the inner sidewall of the upflow reactor, and strip-shaped gaps or through holes are penetrating the surfaces of the upper grid plate 103 and the lower grid plate 104. These strip-shaped gaps or through holes form channels for gas and liquid phases to pass through.

[0047] The above are the basic embodiments of the present invention. Further improvements, optimizations, and limitations can be made to the technical solutions of the present invention based on the above, resulting in the following embodiments:

[0048] Example 2

[0049] This embodiment is an improvement on embodiment 1. Its main structure is the same as that of embodiment 1, but the improvement lies in: [The following is a more detailed description of the improvement.] Figure 1As shown, the receiving cavity 101 has a gas-liquid separator 2 on the downstream side along the flow direction of the gas-liquid mixture. The gas-liquid separator 2 is generally a cylindrical structure with an open top and a closed bottom, or it can be open at the top and closed at the bottom. Regardless of whether the bottom is open or closed, it is fixedly connected to the upper surface of the receiving cavity 101. Its bottom is horizontal, or it can be set as a downward-facing conical cylinder. The center of the gas-liquid separator 2 overlaps with the center of the receiving cavity 101. An overflow channel 201 for the gas-liquid mixture is formed between the side wall of the gas-liquid separator 2 and the edge of the receiving cavity 101. That is, the bottom surface area of ​​the gas-liquid separator 2 is smaller than the upper surface area of ​​the receiving cavity 101. In this way, in terms of installation... When loaded into the upflow reactor, since the side of the receiving cavity 101 is fixedly connected to the inner wall of the reactor, the side wall of the gas-liquid separator 2 forms an annular overflow channel 201 between it and the inner wall of the reactor. The gas-liquid mixture after passing through the receiving cavity 101 will rise along the overflow channel 201. The gas-liquid mixture flows into the gas-liquid separator 2 from the top opening of the gas-liquid separator 2 through the overflow channel 201. The liquid phase is discharged from the liquid phase discharge pipe 202 provided in the upper part of the side wall of the gas-liquid separator 2. One end of the liquid phase discharge pipe 202 extends into the gas-liquid separator 2, and the other end extends out of the reactor. The gas phase is discharged from the top opening of the gas-liquid separator 2.

[0050] Example 3

[0051] An upflow reactor, such as Figure 2 As shown, the upper region of the upflow reactor has the aforementioned flow stabilizer 1, and the channel through which the gas and liquid phases pass in the flow stabilizer 1 is consistent with the material flow direction in the upflow reactor.

[0052] Example 4

[0053] This embodiment is an improvement on embodiment 3. Its main structure is the same as that of embodiment 3, but the improvement lies in: [The following is a more detailed description of the improvement.] Figure 2 As shown, the upflow reactor has a gas-liquid mixture inlet at the bottom, a gas outlet at the top, and a liquid outlet at the top. A scale-collecting inlet diffuser is installed above the gas-liquid mixture inlet, located at the bottom of the upflow hydrogenation reactor. Its main function is to rapidly diffuse the gas-liquid flow across the entire reactor cross-section, preventing the formation of a central flow and back-mixing, thus providing initial distribution. Its structure can utilize any existing inlet diffuser, but the scale-collecting inlet diffuser described below is preferred. This scale-collecting inlet diffuser has a split structure, consisting of three parts, such as... Figure 3As shown, the reactor includes a cylindrical section 3, an arc-shaped guide section 4, and a conical diverter section 5 arranged sequentially from bottom to top along the material flow direction inside the upflow reactor. The cylindrical section 3 is a cylindrical structure arranged around the material inlet of the upflow reactor. The two ends of the cylinder are open, the bottom opening is connected to the material inlet, and a straight channel 301 with the top opening is formed in the middle. In practice, the bottom end of the cylinder is generally welded to the bottom of the upflow reactor and surrounds the material inlet, and its central axis coincides with the central axis of the reactor.

[0054] The arc-shaped flow guide 4 is a cylindrical structure with arc-shaped sidewalls and openings at both ends, and its inner diameter gradually increases from bottom to top. In other words, the arc-shaped flow guide 4 is a frustum-shaped structure with openings at both ends and a hollow interior. Its sidewalls are arc-shaped, bulging away from the center of the reactor. The openings at the top and bottom form channels for material to pass through. In practice, several connecting legs are arranged around the outer sidewall of the arc-shaped flow guide 4. The bottom ends of these connecting legs can be vertically fixed to the bottom wall of the upper flow reactor, or inclined to the bottom wall of the upper flow reactor. Alternatively, they can be vertically or inclinedly fixed to the bottom surface of the upper distribution plate, thereby achieving the fixed installation of the arc-shaped flow guide 4. A reflux channel 7 is formed between the sidewall and the inner wall of the upflow reactor. The reflux channel 7 is annular. The top of the arc-shaped guide section 4 is a certain distance away from the distribution plate inside the upflow reactor. This distance connects with the reflux channel 7, causing some material that does not enter the distributor to turn 180° and flow back when passing through. A baffle 701 is provided in the reflux channel 7. In practice, the baffle 701 generally has two structures. One is a frustum-shaped cylinder with open ends, in which the axis is coaxial with the cylindrical part 3 and surrounds the outer periphery of the cylindrical part 3. The bottom end is fixedly connected to the inner wall of the bottom of the upflow reactor. The inner diameter gradually increases from bottom to top, so that its sidewall forms a certain sharp angle with the inner wall of the bottom of the upflow reactor. The acute angle formed by the inclined plane of the angled surface is the scale collection area 702; another structure is that the baffle 701 is a number of plate-like pieces distributed along the outer wall of the return channel 7, that is, the lower inner wall of the upflow reactor. These plate-like pieces are inclined and not connected to each other, forming a channel. The top end is located in the return channel 7, and the bottom end is fixed to the lower inner wall of the upflow reactor. The width direction of the plate-like pieces forms a certain acute angle with the inner wall of the reactor, which is the scale collection area 702. These plate-like pieces can be at the same height in the reactor or at different heights. One end of the baffle 701 is located in the return channel 7, and the other end is inclinedly and fixedly connected to the inner wall of the upflow reactor. In actual In the process, when the baffle plate 701 is a frustum-shaped cylinder, the top of the cylinder is located in the reflux channel 7 and the bottom is fixed to the bottom wall of the upflow reactor. When the baffle plate 701 is a plate with a certain width, the top of the plate is located in the reflux channel 7 and the bottom is fixed to the bottom wall of the upflow reactor, thus forming a scale collection area 702 with an opening opposite to the flow direction in the reflux channel 7 at the connection. Due to the existence of the reflux channel 7, the flow direction of the material changes by 180°. During this process, the solid particles carried by the material will be thrown to a position close to the lower inner wall of the reactor due to centrifugal force and flow along the reflux channel 7. After being blocked by the baffle plate 701, they will be decelerated and deposited in the scale collection area 702.

[0055] The arc-shaped guide section 4 has an upwardly extending arc-shaped extension cylinder 401 at its bottom opening. In practice, the arc-shaped guide section 4 and the arc-shaped extension cylinder 401 are an integral structure. The arc-shaped extension cylinder 401 forms a variable-diameter flow channel 402 with a diameter that gradually decreases from bottom to top and then gradually increases. A vortex deposition zone 403 is formed between the outer wall of the arc-shaped extension cylinder 401 and the inner wall of the arc-shaped guide section 4. Part of the material flowing through the variable-diameter flow channel 402 in the arc-shaped extension cylinder 401 will change its flow direction due to the obstruction of the upper region of the arc-shaped guide section 4 and flow towards the arc-shaped cavity with an opening formed by the outer wall of the arc-shaped extension cylinder 401 and the inner wall of the lower region of the arc-shaped guide section 4. After hitting the inner wall of the arc-shaped cavity, it flows out along the outer wall of the arc-shaped extension cylinder 401. During the entire flow process, the solid particles carried inside will be thrown onto the inner wall of the vortex deposition zone 403 due to centrifugal force, and thus deposition will occur.

[0056] The conical diversion section 5 is a conical cylindrical structure with its top facing downwards, meaning its large-diameter opening faces upwards. There is a distance between its top and the distribution plate. The conical diversion section 5 is generally fixed in one of three ways: one is by using legs to fix it to the lower surface of the distribution plate; another is by using legs to fix it to the inner wall of the arc-shaped guide section 4; and the third is by using legs to fix it to the inner wall of the reactor. These three fixing methods can be used individually or in combination. A central diversion channel 501 is provided in its center. In practice, the central diversion channel 501 is a through hole. The upper part of the variable diameter flow channel 402 and the outer side wall of the conical diversion section 5 form a guide channel 6. The guide channel 6 and the return channel 7 are connected and cooperate to achieve a 180° turning flow of the material.

[0057] Example 5

[0058] This embodiment further defines the main channel based on embodiment 4. Its main structure is the same as that of embodiment 4, but the improvement is as follows: Figure 3 As shown, the centers of the direct flow channel 301, the variable diameter flow channel 402, the central diversion channel 501, and the material inlet of the upflow reactor are on the same axis, and the diameter of the central diversion channel 501 is smaller than the diameter of the direct flow channel 301, and the diameter of the narrowest point of the variable diameter flow channel 402 is not smaller than the diameter of the direct flow channel 301.

[0059] In this embodiment, the inner diameter of the DC channel 301 is 4-10 times the diameter of the central branch channel 501, the diameter of the narrowest point of the variable diameter channel 402 is 1.2-1.5 times the inner diameter of the DC channel 301, the diameter of the top of the variable diameter channel 402 is 1.5-2 times the inner diameter of the DC channel 301, and the diameter of the bottom of the variable diameter channel 402 is 1.5-2 times the inner diameter of the DC channel 301.

[0060] Example 6

[0061] This embodiment further defines the arc-shaped extension tube 401 based on embodiment 4. Its main structure is the same as that of embodiment 4, but the improvement lies in: Figure 3 As shown, the top of the arc-shaped extension cylinder 401 is lower than the top of the arc-shaped guide section 4, so that some of the material in the guide channel 6 is blocked by the inner wall of the arc-shaped guide section 4 during its flow along the upper inner wall of the arc-shaped extension cylinder 401, forming a backflow that turns towards the eddy deposition zone 403; the bottom diameter of the arc-shaped extension cylinder 401 is larger than the diameter of the cylindrical section 3, so that the material in the return channel 7 is blocked by the outer side of the cylindrical section 3, and flows into the variable diameter channel 402 along the lower inner wall of the arc-shaped extension cylinder 401.

[0062] In this embodiment, the height of the arc-shaped extension cylinder 401 is 30-60% of the height of the arc-shaped guide section 4, and the height of the cylindrical section 3 is 20-30% of the height of the arc-shaped guide section 4; the distance between the arc-shaped extension cylinder 401 and the cylindrical section 3 is 40-60% of the width of the return channel 7.

[0063] Example 7

[0064] This embodiment further defines the conical flow divider 5 based on embodiment 4. Its main structure is the same as in embodiment 4, but the improvement lies in: Figure 3 As shown, the top diameter of the conical diverter 5 is greater than the top diameter of the arc-shaped extension cylinder 401, and the height of the top of the arc-shaped guide 4 is between the bottom and top of the conical diverter 5.

[0065] In this embodiment, the top diameter of the conical diverter 5 is 1.2-1.5 times the top diameter of the arc-shaped extension tube 401, and the height of the top of the arc-shaped guide 4 is located at the upper part of the side wall of the conical diverter 5. This upper part generally refers to the area of ​​60-80% of its height.

[0066] Example 8

[0067] This embodiment further defines the return channel 7 based on embodiment 4. Its main structure is the same as in embodiment 4, but the improvement lies in: Figure 3 As shown, the return channel 7 contains two sets of baffles 701 arranged sequentially along the flow direction. The top of the first set of baffles 701 is higher than the bottom of the arc-shaped guide section 4, and the top of the second set of baffles 701 is closer to the outer wall of the arc-shaped guide section 4 than the top of the first set of baffles 701. The included angle formed by the baffles 701 is generally 30-60°, and the position of their tops is 30-50% of the width of the return channel 7.

[0068] In this embodiment, the width of the reflux channel 7 gradually narrows from top to bottom. In practice, the lower part of the upflow reactor is generally hemispherical, with a material inlet set at its lowest point. At this time, the reflux channel 7 is formed between the outer wall of the arc-shaped guide section 4 and the inner wall of the hemispherical shape. Furthermore, the arc angle of the arc-shaped guide section 4 is adjusted according to the actual situation, so that the width of the reflux channel 7 gradually narrows from top to bottom.

[0069] Example 9

[0070] This embodiment further defines the cylindrical portion 3 based on embodiment 4. Its main structure is the same as in embodiment 4, but the improvement lies in: Figure 3 As shown, the cylindrical part 3 is located in the upflow reactor and forms a flow-blocking component that guides the flow of material in the return channel 7 to change direction. That is, the presence of the cylindrical part 3 can block and guide the flow of material in the return channel 7 to change direction, so that it can better flow into the variable diameter channel 402, and can also play a certain role in deposition, so that some solid particles are deposited at this position.

Claims

1. An upflow reactor, characterized in that: The upper region of the upflow reactor has a flow stabilizer plate (1), and the channel for gas and liquid phases to pass through the flow stabilizer plate (1) is consistent with the material flow direction in the upflow reactor. The flow stabilizer plate (1) includes a spherical body (102) filled in the receiving cavity (101). The two opposite side walls of the receiving cavity (101) have channels for gas-liquid mixtures to pass through. The surface of the spherical body (102) is distributed with several protrusions, which form a gap between two adjacent spherical bodies (102) to buffer the gas-liquid mixture. The bottom of the upflow reactor has a gas-liquid mixture inlet, and a scale-collecting inlet diffuser is provided above the gas-liquid mixture inlet, including a cylindrical part (3), an arc-shaped guide part (4) and a conical diverter part (5) arranged sequentially from bottom to top along the material flow direction. The cylindrical part (3) is a cylindrical structure arranged around the material inlet of the upflow reactor, and a straight channel (301) with an open top is formed in the middle. The arc-shaped guide section (4) is a cylindrical structure with arc-shaped sidewalls and open ends, and its inner diameter gradually increases from bottom to top. A reflux channel (7) is formed between the outer sidewall of the arc-shaped guide section (4) and the inner wall of the upflow reactor. A baffle plate (701) is provided in the reflux channel (7). One end of the baffle plate (701) is in the reflux channel (7), and the other end is inclined and fixedly connected to the inner wall of the upflow reactor, thereby forming a scale collection area (702) with an opening opposite to the flow direction in the reflux channel (7) at the connection. The arc-shaped guide section (4) has an upwardly extending arc-shaped extension cylinder (401) at the bottom opening, and a variable diameter flow channel (402) with a diameter that gradually decreases from bottom to top and then gradually increases is formed inside the arc-shaped extension cylinder (401). A vortex deposition zone (403) is formed between the outer wall of the arc-shaped extension cylinder (401) and the inner wall of the arc-shaped guide section (4). The conical diversion section (5) is a conical cylinder structure with the top of the cone facing downwards, and a central diversion channel (501) is provided in the center of it. A guide channel (6) is formed between the upper part of the variable diameter channel (402) and the outer wall of the conical diversion section (5).

2. The upflow reactor according to claim 1, characterized in that: The centers of the direct flow channel (301), the variable diameter flow channel (402), the central diversion channel (501), and the material inlet of the upflow reactor are on the same axis, and the diameter of the central diversion channel (501) is smaller than the diameter of the direct flow channel (301), and the diameter of the narrowest point of the variable diameter flow channel (402) is not smaller than the diameter of the direct flow channel (301).

3. The upflow reactor according to claim 1, characterized in that: The top of the arc-shaped extension cylinder (401) is lower than the top of the arc-shaped guide section (4), so that some of the material in the guide channel (6) is blocked by the inner wall of the arc-shaped guide section (4) during its flow along the upper inner wall of the arc-shaped extension cylinder (401), forming a backflow that turns towards the eddy deposition zone (403); the bottom diameter of the arc-shaped extension cylinder (401) is larger than the diameter of the cylindrical section (3), so that the material in the return channel (7) is blocked by the outer side of the cylindrical section (3), and flows into the variable diameter channel (402) along the lower inner wall of the arc-shaped extension cylinder (401).

4. The upflow reactor according to claim 1, characterized in that: The top diameter of the conical diverter (5) is greater than the top diameter of the arc-shaped extension tube (401), and the height of the top of the arc-shaped guide (4) is between the bottom and top of the conical diverter (5).

5. The upflow reactor according to claim 1, characterized in that: The return channel (7) has two sets of baffles (701) arranged in sequence along the flow direction of the material. The top of the first set of baffles (701) is higher than the bottom of the arc-shaped guide (4).

6. The upflow reactor according to claim 1, characterized in that: The width of the return channel (7) gradually narrows from top to bottom.

7. The upflow reactor according to claim 1, characterized in that: The cylindrical section (3) is located inside the upflow reactor, forming a flow-blocking component that guides the flow direction of the material in the return channel (7).

8. The upflow reactor according to claim 1, characterized in that: The height of the protrusion is 20-50% of the diameter of the sphere (102).

9. The upflow reactor according to claim 1, characterized in that: The sphere (102) is a solid sphere with a diameter of 5-20 mm and a gap of 1-5 mm between two adjacent spheres (102).

10. The upflow reactor according to claim 1, characterized in that: The containment cavity (101) is a chamber formed by the cooperation of the upper grid plate (103), the lower grid plate (104) and the inner wall of the upflow reactor.

11. The upflow reactor according to claim 1, characterized in that: The receiving cavity (101) has a gas-liquid separation cylinder (2) on the downstream side along the flow direction of the gas-liquid mixture. An overflow channel (201) for the gas-liquid mixture is formed between the side wall of the gas-liquid separation cylinder (2) and the edge of the receiving cavity (101). The gas-liquid mixture flows into the gas-liquid separation cylinder (2) from the top opening through the overflow channel (201). The liquid phase is discharged from the liquid phase discharge pipe (202) provided in the upper part of the side wall of the gas-liquid separation cylinder (2), and the gas phase is discharged from the top opening of the gas-liquid separation cylinder (2).

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