Pulse-sweeping-type gas-phase feed distributor and slurry bed reactor

Abstract

The present invention belongs to the technical field of bubble reactor apparatuses. Provided are a pulse-sweeping-type gas-phase feed distributor and a slurry bed reactor. The pulse-sweeping-type gas-phase feed distributor comprises a first-stage distributor and a second-stage distributor that is arranged below the first-stage distributor and is in mutual communication with the first-stage distributor, wherein the first-stage distributor comprises a first gas distribution disc, a double-layer annular pipe arranged on the outer side of the first gas distribution disc, several gas delivery pipes connecting the first gas distribution disc and the double-layer annular pipe, and several groups of first pulse jet devices uniformly distributed on the double-layer annular pipe; and the second-stage distributor comprises a second gas distribution disc, several dendritic pipes uniformly arranged around the outer edge of the second gas distribution disc, and several groups of second pulse jet devices. Using the double-layer pulse-sweeping-type gas-phase feed distributor of the present invention improves the internal mixing degree of a slurry bed reactor, and also improves the mass transfer reaction efficiency of the slurry bed reactor.

Description

A pulse-sweeping gas-phase feed distributor and a slurry bed reactor Technical Field

[0001] This invention belongs to the technical field of bubble reactor equipment, specifically relating to a pulse-sweeping gas phase feed distributor and a slurry bed reactor. Background Technology

[0002] Due to their advantages such as high transfer efficiency and wide operating range, slurry bed reactors are widely used in process industries involving multiphase catalytic reactions. The internal workings of slurry bed reactors exhibit complex multi-scale coupling behaviors between flow, mass transfer, and reaction, which are significantly influenced by the properties of the medium and internal components. Furthermore, slurry bed reactors can have diameters up to 5 meters. During reactor scale-up, uneven temperature distribution often occurs, leading to adverse consequences such as excessively high local temperature rise, catalyst carbonization or deactivation, and decreased reaction selectivity, thus affecting scale-up results. Therefore, combining slurry bed reactors with highly efficient and strongly mixed heat and mass transfer elements is necessary to solve these problems.

[0003] For slurry bed reactors used in residue hydrotreating, the flow pattern is typically one of co-current upward gas and liquid flow. The size of the bubbles within the reactor significantly impacts the mass transfer interface area and mass transfer coefficient. As one of the most crucial internal components of a slurry bed reactor, the gas distributor directly determines the bubble diameter and initial gas holdup distribution at the reactor inlet, thus influencing the flow behavior in the main reactor region. Currently, research reports on gas distributor structure and bubble distribution patterns are scarce and scattered, with distributor design and optimization primarily relying on experience. Simultaneously, due to requirements such as improving bubble distribution uniformity, optimizing space utilization to reduce dead zones, and reactor scale-up, the structural requirements for distributors are becoming increasingly stringent.

[0004] Smaller bubble sizes result in lower bubble rise velocities, a greater number of bubbles per unit volume, larger bubble specific surface areas, larger gas-liquid interface areas per unit volume, and higher gas content per unit volume. Simultaneously, on a larger scale, the probability of bubble coalescing is lower, maintaining smaller bubble swarm sizes and preventing the formation of excessively large bubbles during flow. The size of the bubble swarm is a range, and according to surface renewal mass transfer theory, a certain proportion of larger bubbles is needed to provide good local turbulence in the liquid, thereby improving the mass transfer coefficient on the liquid side. Therefore, the ideal state inside a slurry bed reactor is the presence of a portion of smaller bubbles to provide sufficient mass transfer interface area, and another portion of larger bubbles to enhance liquid-phase turbulence.

[0005] Patent document CN207463190U discloses a gas distributor and a three-phase slurry bed reactor. The disclosed gas distributor includes an inlet pipe, multiple gas distribution branch pipes, multiple sets of gas distribution ring pipes, and gas nozzles. One end of each gas distribution branch pipe is a blind end, and the other end is connected to the inlet pipe. Both ends of the gas distribution ring pipes are connected to two gas distribution branch pipes respectively. Multiple exhaust holes are provided on both the gas distribution branch pipes and the gas distribution ring pipes, and downward-opening gas nozzles are connected to the exhaust holes. The gas nozzles protrude outwards from the outer walls of the gas distribution branch pipes and the gas distribution ring pipes respectively. This utility model has a simple and reasonable structure, is easy to install and manufacture, and effectively alleviates problems such as catalyst deposition at the bottom of existing reactors and catalyst blockage of the gas distributor when the gas flow pressure is unstable or the gas supply is interrupted. However, this solution does not consider the uniformity of bubble distribution on the lower end cap's arc surface and fails to effectively control the bubble size.

[0006] Based on the current understanding of slurry bed reactors, it is necessary to regulate the size and distribution of bubbles inside the reactor and improve the structure of the corresponding gas phase feed distributor to effectively prevent coking at the bottom of the slurry bed reactor. This is crucial for the efficient conversion and resource utilization of residual oil in my country. Summary of the Invention

[0007] In view of the above problems and related theories, the purpose of this invention is to address the current situation of inaccurate bubble size control and insufficient mixing intensity of the internal flow field in slurry bed reactors. It proposes a pulse-sweeping gas phase feed distributor with adjustable bubble size to enhance heat transfer and mass transfer, thereby enhancing the flow heat transfer to the bottom head, reducing coking, and achieving uniform distribution of small bubbles in the reactor.

[0008] To achieve the above objectives, the present invention adopts the following technical solution:

[0009] A pulse-scanning gas phase feed distributor includes a first-stage distributor and a second-stage distributor disposed below the first-stage distributor; wherein...

[0010] The first-stage distributor includes a first gas distribution disk, a double-layered annular pipe concentrically arranged on the outside of the first gas distribution disk, a plurality of gas delivery pipes connecting the outer wall of the first gas distribution disk and the double-layered annular pipe, and a plurality of first pulse jets evenly distributed on the double-layered annular pipe.

[0011] The second-stage distributor includes a second gas distribution disk, a plurality of tree-shaped pipes evenly arranged around the outer edge of the second gas distribution disk, and a plurality of sets of second pulse jets; each tree-shaped pipe includes a main tree pipe and at least one horizontal secondary tree pipe vertically arranged on the main tree pipe and spaced apart along the length of the main tree pipe, the main tree pipe extending obliquely upward and passing through the secondary tree pipe, and the second pulse jets being evenly distributed on the secondary tree pipe;

[0012] A gas pipe is connected between the first gas distribution plate and the second gas distribution plate, and the gas pipe is connected to the gas inlet pipe connected to the gas source.

[0013] The present invention is further configured such that the air intake pipe is connected to the middle of the gas pipe, so that the gas enters the first-stage distributor and the second-stage distributor evenly.

[0014] The present invention is further configured such that the double-layer annular pipe includes an outer annular pipe and an inner annular pipe arranged concentrically, the inner end of the gas transmission pipe is connected to the outer wall of the first gas distribution disk, and the outer end extends outward and is connected to the inner annular pipe and the outer annular pipe in sequence.

[0015] The present invention is further configured such that each group of first pulse jets includes two first pulse jets symmetrically installed on the double-layer annular pipe with the jet direction downward, and the number of first pulse jets on the outer annular pipe is greater than the number of first pulse jets on the inner annular pipe, so as to ensure a more uniform gas distribution.

[0016] The present invention is further configured such that the number of first pulse jets on the outer annular pipe is 1.2 to 2 times the number of first pulse jets on the inner annular pipe.

[0017] The present invention is further configured such that the two first pulse jets in each group of first pulse jets are inclined toward the inner and outer sides of the double-layer annular pipe, respectively, and the angle between the two first pulse jets and the vertical direction is 25° to 35°.

[0018] The invention is further configured such that the angle between the main branch pipe and the horizontal plane of the second gas distribution disk is 25° to 45°; the outer end of the main branch pipe of each branch pipe extends obliquely upward and passes through the middle of the secondary branch pipe.

[0019] The present invention is further configured such that each group of second pulse jets includes two second pulse jets symmetrically arranged, and the two second pulse jets are symmetrically arranged on the secondary branch pipe with respect to the axial section of the secondary branch pipe perpendicular to the main branch pipe, and the included angle between the two second pulse jets and the axial section of the secondary branch pipe perpendicular to the main branch pipe is 25° to 35°.

[0020] The present invention is further configured such that the number of second pulse jets on the outer layer of the secondary branch pipe is greater than the number of second pulse jets on the inner layer of the secondary branch pipe.

[0021] The present invention is further configured such that the first pulse jet generator and the second pulse jet generator have the same structure, both including an inlet, a main channel and a nozzle that are connected in sequence, and a pair of feedback channels disposed on both sides of the main channel for periodically changing the jet direction of the nozzle, wherein the inlet and outlet of the feedback channels are respectively connected to the inlet and the nozzle.

[0022] The present invention is further configured such that the inlet is a tapered inlet, the nozzle is an umbrella-shaped nozzle, and the spray angle of the nozzle is 100° to 150°.

[0023] As gas passes through the pulse jet injector, it randomly adheres to the feedback channel on one side of the main flow path. The gas in the feedback channel collides with the main flow gas at the outlet, altering the direction of the outlet jet and creating a sweeping flow. Furthermore, due to flow shear and vortex effects, the gas breaks into small bubbles, ultimately causing a periodic change in the rising position of the gas phase within the slurry bed reactor. This promotes gas-liquid backmixing and enhances mass transfer. The periodic sweeping characteristic of the pulse jet injector enables backmixing within the slurry bed reactor.

[0024] The present invention also provides a slurry bed reactor, comprising a slurry bed reactor body and a gas phase feed distributor disposed within the slurry bed reactor body, wherein the gas phase feed distributor is the aforementioned pulse-sweeping gas phase feed distributor. The dimensions of the pulse-sweeping gas phase feed distributor are adaptively adjusted according to the internal dimensions of the slurry bed reactor.

[0025] The present invention is further configured such that the diameter of the slurry bed reactor is D, the diameter of the first gas distribution disk is 0.15D to 0.2D, the diameter of the outer annular pipe is 0.7D to 0.75D, and the diameter of the inner annular pipe is 0.5D to 0.55D.

[0026] The present invention is further configured such that the diameter of the slurry bed reactor is D, the distance between the first gas distribution disk and the second gas distribution disk is H1 = 0.4D to 0.6D, and the distance between the second gas distribution disk and the tangent of the lower end cap of the bottom of the slurry bed reactor is H2 = 0.2D to 0.3D.

[0027] The present invention is further configured such that the diameter of the slurry bed reactor is D, the distance between the innermost branch pipe on the main branch pipe and the second gas distribution disk is 0.2D to 0.25D, and the distance between two adjacent secondary branch pipes is 0.2D to 0.25D.

[0028] The length of the main branch pipe of the second-stage distributor is 0.45D to 0.5D, and the length of the secondary branch pipe is 0.2D to 0.25D.

[0029] The present invention is further configured to include four tree-shaped pipes evenly arranged around the outer edge of the second gas distribution disk, each tree-shaped pipe including one main tree pipe and two secondary tree pipes spaced apart along the length of the main tree pipe.

[0030] The present invention is further configured such that the gas velocity at the nozzle of each of the first and second pulse jet nozzles is 5-12 m / s, the flow rate is 0.6-2.6 m³ / h, and the scanning area is 0.01 m². 2 -0.015m 2 Compared to ordinary gas nozzles, the gas coverage area is increased by 50%-150%, and the bubble distribution is more uniform. The pulse jet generator produces microbubble clusters with diameters of 10 to 10,000 micrometers, and the size distribution exhibits a quasi-normal distribution. The microbubble clusters rise with the flow of the liquid phase and are redistributed on the cross-section of the reactor.

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

[0032] (1) The gas phase feed distributor designed in this invention combines annular pipe and tree-shaped pipe and applies pulse sweep jet to diffuse the gas evenly in the lower space of the gas distributor, without material accumulation dead corners; it can effectively improve the problem of uneven gas distribution in traditional gas distributors that enter from one side, and significantly increase the uniformity of micro bubbles in the reactor.

[0033] (2) This invention utilizes a pulse-sweeping jet injector, which, by leveraging the inherent flow instability mechanism, can convert a stable jet into an oscillating jet, achieving full-area sweeping spray coverage of the slurry bed's lower head structure. This enhances flow heat transfer, reduces coking at the lower head, and strengthens the mixing between the gas and liquid phases. Compared to ordinary bubble nozzles, the gas coverage area of ​​a single pulse-sweeping jet injector is increased by 50%-150%, thereby reducing the number of gas phase distributor nozzles required.

[0034] (3) The gas phase feed distributor designed in this invention has a number of pulse jets that can be increased or decreased according to process conditions. The distributor has a simple pipeline structure, is easy to manufacture and disassemble, provides uniform gas distribution, and is easy to clean. Attached Figure Description

[0035] Figure 1 is a schematic diagram of a slurry bed reactor equipped with a pulse-sweeping gas phase feed distributor.

[0036] Figure 2 is a front view of the first-level distributor.

[0037] Figure 3 is a bottom view of Figure 2.

[0038] Figure 4 is a front view of the second-level distributor.

[0039] Figure 5 is a bottom view of Figure 4.

[0040] Figure 6 illustrates the structure of the pulse jet generator and compares its sweeping range with that of a conventional gas-phase feeder. The left side shows the pulse jet generator, and the right side shows the conventional gas-phase feeder.

[0041] Figure 7 is a schematic diagram of the reverse mixing effect inside the slurry bed reactor.

[0042] Among them, 1. Slurry bed reactor body, 2. Inlet pipe, 100. First-stage distributor, 110. First gas distribution plate, 120. Double-layer annular pipe, 121. Inner annular pipe, 122. Outer annular pipe, 130. Gas delivery pipe, 140. First pulse jet, 141. Inlet, 142. Main channel, 143. Nozzle, 144. Feedback channel, 200. Second-stage distributor, 210. Second gas distribution plate, 220. Tree-shaped pipe, 221. Main tree-shaped pipe, 222. Secondary tree-shaped pipe, 230. Second pulse jet, 300. Gas pipe. Detailed Implementation

[0043] The technical solution of the present invention will be clearly and completely described below with reference to specific embodiments. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments.

[0044] Example 1

[0045] Referring to Figures 1 to 5, this embodiment provides a pulse-sweeping gas phase feed distributor, which includes a first-stage distributor 100, a second-stage distributor 200 disposed below the first-stage distributor 100, and a gas pipeline 300 for connecting the first-stage distributor 100 and the second-stage distributor 200; wherein,

[0046] The first-stage distributor 100 includes a first gas distribution disk 110, a double-layer annular pipe 120 concentrically arranged on the outside of the first gas distribution disk 110, a plurality of gas delivery pipes 130 connecting the outer wall of the first gas distribution disk 110 and the double-layer annular pipe 120, and a plurality of first pulse jets 140 evenly distributed on the double-layer annular pipe 120.

[0047] The second-stage distributor 200 includes a second gas distribution disk 210, four tree-shaped pipes 220 evenly arranged around the outer edge of the second gas distribution disk 210, and several sets of second pulse jets 230; each tree-shaped pipe 220 includes a main tree pipe 221 and two horizontal secondary tree pipes 222 vertically arranged on the main tree pipe 221 and spaced apart along the length of the main tree pipe 221; the main tree pipe 221 extends obliquely upward and passes through the middle of the secondary tree pipes 222; the second pulse jets 230 are evenly distributed on the secondary tree pipes 222 on both sides of the main tree pipe 221.

[0048] The two ends of the gas pipe 300 are respectively connected to the bottom of the first gas distribution plate 110 and the top of the second gas distribution plate 210. The gas pipe 300 is connected to the gas inlet pipe 2 connected to the gas source, and the gas inlet pipe 2 is connected to the middle of the gas pipe 300.

[0049] The double-layer annular pipe 120 includes an inner annular pipe 121 and an outer annular pipe 122 arranged concentrically. The inner end of the gas transmission pipe 130 is connected to the outer wall of the first gas distribution disk 110, and the outer end extends outward and is connected to the inner annular pipe 121 and the outer annular pipe 122 in sequence.

[0050] Each group of first pulse jets includes two first pulse jets 140 symmetrically mounted on the double-layer annular pipe 120 with the jet direction downward. The two first pulse jets 140 are respectively inclined towards the inner and outer sides of the double-layer annular pipe 120; and the angle between the first pulse jet 140 and the vertical direction is 25° to 35°.

[0051] The number of first pulse jets 140 on the outer annular pipe 122 is 1.2 to 2 times the number of first pulse jets 140 on the inner annular pipe 121.

[0052] The angle between the main branch pipe 221 of each of the tree-shaped pipes 220 and the horizontal plane of the second gas distribution disk 210 is 25° to 45°.

[0053] Each group of second pulse jets includes two symmetrically arranged second pulse jets 230. The two second pulse jets 230 are symmetrically arranged on the secondary branch pipe 222 with respect to the axial section of the secondary branch pipe 222 perpendicular to the main branch pipe 221. The included angle between the two second pulse jets 230 and the axial section of the secondary branch pipe 222 perpendicular to the main branch pipe 221 is 25° to 35°.

[0054] The number of second pulse jets 230 on the outer secondary branch pipe 222 is greater than the number of second pulse jets on the inner branch pipe 222. The number of second pulse jets 230 on the outer secondary branch pipe 222 is 1.2 to 2.0 times the number of second pulse jets on the inner branch pipe 222.

[0055] Referring to Figure 6, the first pulse jet ejector 140 and the second pulse jet ejector 230 have the same structure. The first pulse jet ejector 140 includes an inlet 141, a main channel 142, and a nozzle 143 connected sequentially from top to bottom, as well as a pair of feedback channels 144 disposed on both sides of the main channel 142 for periodically changing the jet direction of the nozzle 143. The inlet end and outlet end of the feedback channel 144 are respectively connected to the inlet 141 and the nozzle 143. The inlet 141 is a tapered inlet, the nozzle 143 is an umbrella-shaped outlet, and the nozzle angle of the nozzle 143 is 100° to 150°.

[0056] The inlet 141 of the first pulse jet injector 140 is connected to the double-layer annular pipe 120, and the inlet 141 of the second pulse jet injector 230 is connected to the secondary tree pipe 222. After entering the pulse jet injector through the inlet 141, the gas velocity increases significantly. Most of the gas carries considerable kinetic energy and flows through the main channel 142, then is ejected through the nozzle 143. A small portion of the gas enters the feedback channel 144 and intermittently flows back to the main channel 142, causing instantaneous disturbances and changes in the airflow within the main channel 142. These disturbances and changes occur intermittently and periodically, affecting the position of the small-sized bubbles ejected from the nozzle, forming a stable pulsed sweeping frequency. Because the gas-phase pulse sweeping position of the pulse jet injector changes over time, different gas-phase rising positions are formed in the slurry bed reactor body 1, promoting full gas-liquid mixed circulation and enhancing reaction mass transfer. In contrast, traditional gas-phase feeders, lacking an internal feedback channel, have a smaller gas sweeping range. Compared to traditional gas phase feeders, the effective coverage area of ​​the pulse jet gas sweeping of this invention can be increased by 50%-150%.

[0057] As shown in Figure 7, the periodic sweeping characteristic of the pulse jet realizes the gas back-mixing process inside the slurry bed reactor, which helps to enhance the mixing between the gas and liquid phases and improve the mass transfer effect.

[0058] This embodiment also provides a slurry bed reactor, including a slurry bed reactor body 1 and the aforementioned pulse-scanning gas phase feed distributor disposed within the slurry bed reactor body 1.

[0059] The diameter of the slurry bed reactor is D, and the distance H1 between the first gas distribution disk 110 and the second gas distribution disk 210 is 0.4D to 0.6D; the distance H2 between the second gas distribution disk 210 and the tangent of the lower end cap at the bottom of the slurry bed reactor is 0.2D to 0.3D.

[0060] The length of the main branch pipe 221 of the second-stage distributor 200 is 0.45D to 0.50D, and the length of the secondary branch pipe 222 is 0.2D to 0.25D; the distance between the secondary branch pipe 222 on the inner layer of the main branch pipe 221 and the second gas distribution disk 210 is 0.2D to 0.25D; the distance between two adjacent secondary branch pipes 222 is 0.2 to 0.25D.

[0061] Example 2

[0062] In this embodiment, the cross-sectional bubble coverage caused by the pulse-sweeping gas phase feed distributor with different numbers of main branch pipes in Embodiment 1 was simulated. In this embodiment, the angle between the main branch pipe 221 and the second gas distribution disk 210 is 45°, and the length is 0.45D. The length of the secondary branch pipe 222 is 0.2D. The number of second pulse jets 230 on the outer layer branch pipe 222 is 1.5 times that on the inner layer branch pipe. The simulated number of main branch pipes and the corresponding number of pulse jets, as well as the resulting cross-sectional bubble coverage results, are shown in Table 1. The spray area coverage refers to the coverage area of ​​the bubbles on the lower end cap surface.

[0063] Table 1. Bubble coverage results for different numbers of main branch pipes

[0064] As can be seen from the results in Table 1, when the number of main branch pipes is 4, excellent cross-sectional bubble coverage is achieved while using a smaller number of pulse jets.

[0065] Application examples

[0066] The original gas-phase feed device in the slurry bed reactor of a petrochemical plant used a conventional bubbling reactor component to hydrogenate residual oil, with hydrogen transported through a gas-phase main pipe. Now, ensuring all other conditions remain the same, the original bubbling reactor component will be replaced with the pulse-sweeping gas-phase feed distributor provided in Example 1. The second-stage gas-phase distributor of the pulse-sweeping gas-phase feed distributor includes one gas distribution disk and four symmetrically distributed tree-shaped pipes 220. Each tree-shaped pipe 220 includes a main tree pipe 221 and two secondary tree pipes 222 located on the main tree pipe 221. The inner secondary tree pipes 222 are equipped with four sets of second pulse jets 230, and the outer secondary tree pipes 222 are equipped with six sets of second pulse jets 230. The injection angle of each pulse jet nozzle 143 is 120°, the gas velocity at the outlet is 5 m / s-12 m / s, the flow rate is 0.6-2.6 m³ / h, and the single nozzle sweeping cycle is 0.005 s-0.01 s. The reaction parameters and bubble results are as follows:

[0067] Table 2 Results of slurry bed reactors using pulse-scanned gas-phase feed distributors and conventional bubble reactor internals.

[0068] As can be seen from the data in Table 2, under the same operating conditions, using the pulse-sweeping gas phase feed distributor provided by this invention as the gas phase feed device results in smaller average bubble diameter and larger average bubble specific surface area compared to using traditional bubbling reactor internals. In other words, the more microbubbles there are, the higher the average gas content. Therefore, the hydrogen-to-oil volume ratio is significantly lower than that of existing bubbling reactors, and the residue-to-oil conversion rate is also higher. Furthermore, after long-term operation of the reactor, it was found that the coking situation using the pulse-sweeping gas phase feed distributor is better than that of traditional bubbling reactor internals.

[0069] The specific embodiments of the present invention have been described in detail above, but they are only examples, and the present invention is not limited to the specific embodiments described above. For those skilled in the art, any equivalent modifications and substitutions to this utility model are also within the scope of the present invention. Therefore, all equivalent changes and modifications made without departing from the spirit and scope of the present invention should be covered within the scope of the present invention.

Claims

1. A pulse-sweeping gas phase feed distributor, characterized in that, It includes a first-level distributor that is interconnected with the first-level distributor and a second-level distributor located below the first-level distributor; wherein, The first-stage distributor includes a first gas distribution disk, a double-layered annular pipe concentrically arranged on the outside of the first gas distribution disk, a plurality of gas delivery pipes connecting the outer wall of the first gas distribution disk and the double-layered annular pipe, and a plurality of first pulse jets evenly distributed on the double-layered annular pipe. The second-stage distributor includes a second gas distribution disk, a plurality of tree-shaped pipes uniformly arranged around the outer edge of the second gas distribution disk, and a plurality of second pulse jets arranged on the tree-shaped pipes; each tree-shaped pipe includes a main tree pipe and at least one horizontal secondary tree pipe arranged vertically on the main tree pipe and spaced apart along the length of the main tree pipe, the main tree pipe extending obliquely upward and passing through the secondary tree pipe; A gas pipe is connected between the first gas distribution plate and the second gas distribution plate, and the gas pipe is connected to the gas inlet pipe connected to the gas source.

2. The pulse-sweeping gas phase feed distributor according to claim 1, characterized in that, The double-layer annular pipe includes an outer annular pipe and an inner annular pipe arranged concentrically. The inner end of the gas transmission pipe is connected to the outer wall of the first gas distribution disk, and the outer end extends outward and is connected to the inner annular pipe and the outer annular pipe in sequence. Each group of first pulse jets includes two first pulse jets symmetrically mounted on the double-layer annular pipe with the jet direction downward. The number of first pulse jets on the outer annular pipe is greater than the number of first pulse jets on the inner annular pipe.

3. A pulse-sweeping gas phase feed distributor according to claim 2, characterized in that, The two first pulse jets are respectively inclined toward the inner and outer sides of the double-layer annular pipe, and the angle between the first pulse jets and the vertical direction is 25° to 35°.

4. A pulse-sweeping gas phase feed distributor according to claim 1, characterized in that, The angle between each of the main branch pipes and the horizontal plane of the second gas distribution plate is 25° to 45°, and the outer end of the main branch pipe of each of the branch pipes extends obliquely upward and passes through the middle of the secondary branch pipe.

5. A pulse-sweeping gas phase feed distributor according to claim 1, characterized in that, Each group of second pulse jets includes two symmetrically arranged second pulse jets, and the two second pulse jets are symmetrically arranged on the secondary branch pipe with respect to the axial section of the secondary branch pipe perpendicular to the main branch pipe. The included angle between the two second pulse jets and the axial section of the secondary branch pipe perpendicular to the main branch pipe is 25° to 35°.

6. A pulse-sweeping gas phase feed distributor according to claim 1, characterized in that, The first pulse jet generator and the second pulse jet generator have the same structure, both including an inlet, a main channel and a nozzle that are connected in sequence, and a pair of feedback channels located on both sides of the main channel for periodically changing the jet direction of the nozzle. The inlet and outlet of the feedback channels are respectively connected to the inlet and the nozzle.

7. A pulse-sweeping gas phase feed distributor according to claim 6, characterized in that, The inlet is a tapered inlet, the nozzle is an umbrella-shaped nozzle, and the spray angle of the nozzle is 100° to 150°.

8. A slurry bed reactor, characterized in that, The reactor includes a slurry bed reactor body and a gas phase feed distributor disposed within the slurry bed reactor body, wherein the gas phase feed distributor is a pulse-sweeping gas phase feed distributor as described in any one of claims 1 to 7.

9. A slurry bed reactor according to claim 8, characterized in that, The diameter of the slurry bed reactor is D, and the distance between the first gas distribution disk and the second gas distribution disk is H1 = 0.4D to 0.6D; the distance between the second gas distribution disk and the tangent of the lower end cap at the bottom of the slurry bed reactor is H2 = 0.2D to 0.3D.

10. A slurry bed reactor according to claim 8, characterized in that, The diameter of the slurry bed reactor is D; the distance between the innermost branch pipe on the main branch pipe and the second gas distribution disk is 0.2D to 0.25D; the distance between two adjacent secondary branch pipes is 0.2D to 0.25D. The length of the main branch pipe of the second-stage distributor is 0.45D to 0.50D, and the length of the secondary branch pipe is 0.2D to 0.25D.

11. A slurry bed reactor according to claim 8, characterized in that, Four tree-shaped pipes are evenly arranged around the outer edge of the second gas distribution disk. Each tree-shaped pipe includes one main tree pipe and two secondary tree pipes spaced apart along the length of the main tree pipe.

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