Hydroprocessing reactor and its inlet diffuser

Abstract

This invention discloses an inlet diffuser, comprising: a sleeve consisting of an inner cylinder and an outer cylinder arranged coaxially, the bottom end of the inner cylinder being higher than the bottom end of the outer cylinder, with a liquid-holding zone between the inner and outer cylinders; an annular bottom plate coaxially connected to the bottom end of the outer cylinder, forming a liquid phase channel between the annular bottom plate and the inner cylinder, the area of ​​the liquid phase channel being less than or equal to the area of ​​the liquid-holding zone; a top cover disposed above the inner cylinder, forming a gas phase channel between the top cover and the inner cylinder; a rotating shaft coaxially inserted into the inner cylinder; at least one layer of helical blades disposed within the inner cylinder and driving the rotating shaft to rotate; and at least one layer of splash plates, which have a downward-opening conical structure, and the splash plates are linked to the lower end of the rotating shaft. This invention also discloses a hydrogenation reactor. In the inlet diffuser of this invention, the gas phase enters the inner cylinder, blowing the helical blades and driving the splash plates to rotate, providing an initial horizontal velocity to the liquid phase, and covering the entire reactor cross-section with a spray area.

Description

Technical Field

[0001] This invention relates to the field of hydrogenation reaction equipment technology, especially hydrogenation reaction equipment with a large reactor scale, and particularly to a hydrogenation reactor and its inlet diffuser. Background Technology

[0002] In recent years, with rapid economic development and increased environmental awareness, the requirements for the quality and environmental protection of petrochemical products have become increasingly stringent. As one of the technological means to produce clean fuels, hydrogenation technology is playing an increasingly important and significant role in the oil refining industry. In hydrogenation units, along with hydrogenation catalyst technology and hydrogenation process technology, the internal components technology of the hydrogenation reactor is also an important part of the reaction system. These three factors constitute the three key factors affecting reactor performance.

[0003] Hydrogenation is an exothermic reaction. Uneven material distribution can lead to more vigorous reactions in areas where the catalyst is well-wetted, with faster reaction rates generating more heat and affecting the radial temperature difference of the reactor. When the radial temperature difference is large, localized hot spots form, causing premature catalyst deactivation and impairing catalyst performance. This can even lead to coking and caking in certain areas, preventing normal material flow. Since fixed-bed hydrogenation reactors operate in a trickle-bed flow pattern, the catalyst below the caking area cannot function, significantly reducing catalyst lifespan and unit uptime. Furthermore, localized caking increases the catalyst bed pressure drop, passively raising the reactor's operating pressure. This increases energy consumption and poses a risk to stable unit operation. If the pressure drop rises too rapidly to the reactor's design value, an abnormal shutdown is necessary for remedial measures, incurring additional maintenance costs. Additionally, catalyst sieving leads to catalyst loss and waste.

[0004] In a hydrotreating unit, the hydrotreating reactor, a key piece of equipment, undergoes refining and cracking reactions on feedstock oil mixed with hydrogen in a specific ratio, aided by a hydrotreating catalyst. The stable operation of the hydrotreating reaction within the reactor, the full effectiveness of the hydrotreating catalyst, and the achievement of high-quality products largely depend on the uniformity of the gas-liquid phase distribution within the catalyst bed. The inlet diffuser, as the first component into the reactor, serves two purposes: firstly, to promote uniform mixing of the gas and liquid phases through agitation; and secondly, to diffuse the gas and liquid phases across the entire cross-section, eliminating their vertical impact on the top distribution plate and creating stable operating conditions for the distribution plate. The uniformity of the gas-liquid phase distribution within the catalyst bed is closely related to the design of the hydrotreating reactor's internal components. It can be said that the performance of these internal components directly affects catalyst life, product quality, and the unit's operating cycle; using high-performance internal components in a hydrotreating reactor is tantamount to replacing the catalyst with one of higher activity.

[0005] Patent document CN106268524A discloses a diffuser and a fixed-bed reactor. The diffuser is located at the inlet of the reactor body and includes a cylindrical body and a swirl plate disposed within the cylindrical body. A gas-liquid material inlet is located at the top of the cylindrical body, and a gas-liquid material diffusion port is located on the bottom side. The swirl plate is a curved panel extending axially along the cylindrical body to the gas-liquid material diffusion port. Patent document CN205495530U discloses a swirl-type inlet diffuser, including a coaxially connected cylindrical body, a buffer plate, a cover plate, and a flow-breaking plate. A flange is welded to the top of the cylindrical body, and a bottom plate with a centrally located circular outlet is installed at the bottom of the cylindrical body. Several spirally arranged guide plates are fixed on the bottom plate, forming a centrally cylindrical mixing chamber as a channel for the gas-liquid medium. This diffuser has advantages such as strong buffering effect, thorough gas-liquid mixing, and a large liquid phase spray area. It can reduce the peak value of the liquid phase radial distribution and uniformly diffuse the gas-liquid medium across the entire reactor cross-section, creating conditions for the stable conduction of the catalytic hydrogenation reaction.

[0006] As hydrogenation units gradually move towards larger scales, existing technologies face significant challenges in addressing this trend. Firstly, because the inlet of the hydrogenation reactor needs to be connected to a pipeline, its diameter has an upper limit and cannot be arbitrarily increased with reactor diameter growth. Currently, the ratio of reactor diameter to inlet diameter has reached over 10 times. Traditional inlet diffusers often use a gas-liquid entrainment method to distribute the medium, expanding the spray area of ​​the liquid material across the entire reactor cross-section. However, from a fluid motion perspective, when the gas phase enters the reactor from the inlet diffuser, its accumulation velocity rapidly decreases due to the significant difference between the reactor diameter and the inlet pipeline diameter. Furthermore, once the liquid phase loses the continuous propulsion of the gas phase, it quickly slides down under gravity. Even with different types of splash plate structures, it is still impossible to meet the material distribution area requirements of large-scale hydrogenation reactors.

[0007] Secondly, traditional inlet distributors mostly employ a fixed structure, lacking the ability to adapt to fluctuations in material flow rate. That is, once the structural parameters are determined, the actual spray area of ​​the liquid phase is only affected by the liquid phase velocity, meaning it is entirely determined by the liquid phase quantity. In actual operation, the liquid phase feed rate is constantly fluctuating, typically failing to reach the upper limit of the flow velocity within the pipe, preventing the inlet diffuser from achieving stable, long-term full-load operation. When the liquid phase quantity decreases, the flow velocity decreases accordingly, causing the spray area to converge towards the central region of the hydrogenation reactor, thus reducing the service area and failing to create stable working conditions for the top distribution plate.

[0008] The information disclosed in this background section is intended only to enhance the understanding of the overall background of the invention and should not be construed as an admission or in any way implying that the information constitutes prior art known to those skilled in the art. Summary of the Invention

[0009] One of the objectives of this invention is to provide a hydrogenation reactor and its inlet diffuser, thereby improving the problem of insufficient spraying area of ​​liquid phase materials in ultra-large hydrogenation reactors.

[0010] To achieve the above objectives, according to a first aspect of the present invention, an inlet diffuser is provided, comprising: a sleeve consisting of an inner cylinder and an outer cylinder arranged coaxially, the bottom end of the inner cylinder being higher than the bottom end of the outer cylinder, and a liquid holding area between the inner cylinder and the outer cylinder; an annular bottom plate coaxially connected to the bottom end of the outer cylinder, forming a liquid phase channel between the annular bottom plate and the inner cylinder, the area of ​​the liquid phase channel being less than or equal to the area of ​​the liquid holding area; a top cover disposed above the inner cylinder, forming a gas phase channel between the top cover and the inner cylinder; a rotating shaft coaxially passing through the inner cylinder, the lower end of the rotating shaft passing through the annular bottom plate; at least one layer of spiral blades disposed within the inner cylinder and driving the rotating shaft to rotate; and at least one layer of splash plates having a downward-opening conical structure, the splash plates being linked to the lower end of the rotating shaft.

[0011] Furthermore, in the above technical solution, the cone angle of each splash plate is 90 to 180°.

[0012] Furthermore, in the above technical solution, each splash plate is composed of multiple fan-shaped plates distributed at intervals, and the number of fan-shaped plates in each splash plate is 3 to 8.

[0013] Furthermore, in the above technical solution, the outer end of the fan-shaped piece is provided with serrations.

[0014] Furthermore, in the above technical solution, the outer edge of the fan-shaped piece extends into a horizontal section.

[0015] Furthermore, in the above technical solution, when two splash plates are provided, the fan-shaped blades of the upper splash plate and the fan-shaped blades of the lower splash plate are arranged alternately.

[0016] Furthermore, in the above technical solution, when two splash plates are provided, the cone angle of the upper splash plate is greater than the cone angle of the lower splash plate.

[0017] Furthermore, in the above technical solution, the splash plate is provided with multiple liquid drop holes.

[0018] Furthermore, in the above technical solution, multiple liquid-falling holes are distributed along concentric circles with the rotating shaft as the center.

[0019] Furthermore, in the above technical solution, the number of each layer of spiral blades is 3 to 5; the windward side of the spiral blades is in the axial direction, and the blade angle is 50 to 78°.

[0020] Furthermore, in the above technical solution, the top cover is a conical, spherical, or flat structure.

[0021] Furthermore, in the above technical solution, the inner cylinder is equipped with a bearing bracket, and the rotating shaft is connected to the inner cylinder through the bearing bracket.

[0022] Furthermore, in the above technical solution, the inner cylinder is provided with multiple upper support legs and multiple lower support legs. The inner cylinder is connected to the annular bottom plate through the lower support legs, and the top cover is connected to the upper end of the inner cylinder through the upper support legs.

[0023] Furthermore, in the above technical solution, the inner diameter of the annular bottom plate is 0.6 to 1.0 times the diameter of the inner cylinder.

[0024] According to a second aspect of the present invention, a hydrogenation reactor is provided, comprising: a body having a cylindrical structure and a feed inlet at the center of the upper end of the body; and an inlet diffuser as described in any of the above technical solutions, disposed at the feed inlet.

[0025] Furthermore, in the above technical solution, the diameter of the main body is greater than or equal to 6.5m.

[0026] Compared with the prior art, the present invention has the following beneficial effects:

[0027] 1. The inlet diffuser of this invention, through its movable internal components, fundamentally changes the working principle of the inlet diffuser, enabling the distribution of the liquid phase within a large-scale hydrogenation reactor after being sprayed through a small-diameter pipe. The gas phase enters the inner cylinder through the gas phase channel between the inner cylinder and the top cover. The forward-blowing helical blades drive the rotating shaft to rotate, fully utilizing the kinetic energy of the liquid phase flowing through the inner cylinder. This further drives the splash plate below the rotating shaft to rotate, thereby forming a stable centrifugal force field. This provides the liquid phase with an initial horizontal velocity, slowing down its sliding velocity under gravity, and covering the entire reactor cross-section with the spray area, meeting the requirements for large-scale equipment.

[0028] 2. The inlet diffuser of this invention is powered primarily by the kinetic energy of the gas flow, making it suitable for materials with high gas content. It is less affected by the liquid flow rate, and can achieve long-term stable operation while ensuring a stable gas flow rate. When the liquid flow rate decreases, i.e., when the liquid feed rate is at a low point, the spray area will not shrink towards the center of the hydrogenation reactor, and the service area will remain stable. This creates stable working conditions for the top distribution plate and demonstrates strong adaptability to fluctuations in liquid flow rate.

[0029] 3. In the inlet diffuser of this invention, the helical blades on the main shaft are located inside the inner cylinder, making full use of the large amount of kinetic energy possessed by the gas phase at this location. This energy is first converted into mechanical energy for the rotation of the shaft, and then transferred to the liquid phase through the collision of the splash plate with the liquid phase. This avoids the problem in traditional inlet diffusers where the large difference between the reactor diameter and the inlet pipe diameter causes the energy accumulated in the gas phase after entering the reactor to rapidly decay, preventing the liquid phase from receiving continuous propulsion from the gas phase. This has positive significance in the rational utilization of energy.

[0030] 4. When the inlet diffuser of the present invention is in operation, the liquid phase flows out from the center of the annular bottom plate and enters the reactor through the downcomers opened at different positions of the splash plate or through the gaps between adjacent fan-shaped plates, obtaining different horizontal initial velocities and forming a liquid phase distribution along the entire cross-section of the reactor. At the same time, through the horizontal section extending from the outer edge of the splash plate, the liquid phase detached from the edge of the splash plate will not generate a vertical velocity component, thereby prolonging the time for the material to fall to the top distribution plate, thus enabling a wider liquid phase coverage area.

[0031] The above description is merely an overview of the technical solution of the present invention. In order to better understand the technical means of the present invention and to implement it according to the contents of the specification, and to make the above and other objects, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with reference to the accompanying drawings. Attached Figure Description

[0032] Figure 1 This is a schematic diagram of the structure of an inlet diffuser according to an embodiment of the present invention.

[0033] Figure 2 This is a schematic diagram of the structure of an inlet diffuser according to another embodiment of the present invention.

[0034] Figure 3 This is a top view of the splash plate according to another embodiment of the present invention.

[0035] Explanation of key figure labels:

[0036] 120-Inlet diffuser, 121-Inner cylinder, 1211-Lower support leg, 1212-Upper support leg, 1213-Bearing bracket, 122-Outer cylinder, 123-Annular base plate, 124-Top cover, 125-Rotating shaft, 126-Helical blade, 127-Splash plate.

[0037] 220-Inlet diffuser, 221-Inner cylinder, 2211-Lower support leg, 2212-Upper support leg, 2213-Bearing bracket, 222-Outer cylinder, 223-Annular bottom plate, 224-Top cover, 225-Rotating shaft, 226-Helical blade, 227-Splash plate, 2270-Fan-shaped blade, 2271-Horizontal section, 2272-Downcomer hole. Detailed Implementation

[0038] The specific embodiments of the present invention will now be described in detail with reference to the accompanying drawings, but it should be understood that the scope of protection of the present invention is not limited to the specific embodiments.

[0039] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0040] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “up,” etc., are used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation, in addition to those depicted in the figures. For example, if an object in the figure is flipped, an element described as “below” or “under” another element or feature would be oriented “above” that element or feature. Thus, the exemplary term “below” can encompass both the downward and upward orientations. An object may also have other orientations (rotated 90 degrees or other orientations), and the spatial relative terms used herein should be interpreted accordingly.

[0041] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0042] A hydrogenation reactor (not shown in the figure) according to a specific embodiment of the present invention includes a cylindrical body with a feed inlet at the center of the upper end of the body. An inlet diffuser according to the present invention is provided at the feed inlet.

[0043] Furthermore, in one or more exemplary embodiments of the present invention, the hydrogenation reactor refers to an ultra-large hydrogenation reactor with a body diameter greater than or equal to 6.5m.

[0044] like Figure 1As shown, the inlet diffuser 120 according to a specific embodiment of the present invention includes a sleeve composed of an inner cylinder 121 and an outer cylinder 122 arranged coaxially. The bottom end of the inner cylinder 121 is higher than the bottom end of the outer cylinder 122, and a liquid holding area is formed between the inner cylinder 121 and the outer cylinder 122. An annular bottom plate 123 is coaxially connected to the bottom end of the outer cylinder 122, and a liquid phase channel is formed between the annular bottom plate 123 and the inner cylinder 121. The distance between the bottom end of the inner cylinder 121 and the annular bottom plate 123 is such that the area of ​​the liquid phase channel is less than or equal to the area of ​​the liquid holding area. Exemplarily, the outer periphery of the annular bottom plate 123 can be welded to the bottom end of the outer cylinder 122. A top cover 124 is provided above the inner cylinder 121, and a gas phase channel is formed between the top cover 124 and the inner cylinder 121. A rotating shaft 125 is coaxially inserted in the inner cylinder 121, and the lower end of the rotating shaft 125 passes through the annular bottom plate 123. A helical blade 126 is provided on the rotating shaft 125. The helical blade 126 is disposed inside the inner cylinder 121 and drives the rotating shaft 125 to rotate. A splash plate 127 is connected to the lower end of the rotating shaft 125 in a linked manner. The splash plate 127 has a cone-shaped structure with its opening facing downwards. It should be understood that... Figure 1 The spiral blade 126 and the splash plate 127 shown are both single layers. However, this invention is not limited to this. Those skilled in the art can select the number of layers of spiral blades and splash plates according to actual needs.

[0045] Furthermore, in one or more exemplary embodiments of the present invention, the cone angle of the splash plate 127 may be 90 to 180°.

[0046] Furthermore, in one or more exemplary embodiments of the present invention, the splash plate 127 may be composed of a plurality of fan-shaped pieces spaced apart, with each layer of the splash plate having 3 to 8 fan-shaped pieces. Furthermore, in one or more exemplary embodiments of the present invention, the outer ends of the fan-shaped pieces may be provided with serrations.

[0047] Furthermore, in one or more exemplary embodiments of the present invention, the number of each layer of helical blades 126 can be 3 to 5. Furthermore, in one or more exemplary embodiments of the present invention, the windward surface of the helical blades is axial, and the blade angle is 50 to 78°.

[0048] Furthermore, in one or more exemplary embodiments of the present invention, such as Figure 1 As shown, the top cover 124 can be conical. It should be understood that the present invention is not limited to this, and the top cover can also be spherical or flat.

[0049] Furthermore, in one or more exemplary embodiments of the present invention, the inner wall of the inner cylinder 121 is provided with a bearing support 1213, including an upward-opening bearing seat and a support leg. A bearing is mounted on the rotating shaft 125 and is correspondingly placed in the bearing seat, with the outer ring fixed to the inner wall of the inner cylinder 121 as a retaining ring.

[0050] Furthermore, in one or more exemplary embodiments of the present invention, the lower end of the inner cylinder 121 can be connected to the annular bottom plate 123 via the lower support leg 1211, and the gap between the two is a liquid phase channel. The upper end of the inner cylinder 121 can be connected to the top cover 124 via the upper support leg 1212, and the gap between the two is a gas phase channel.

[0051] Furthermore, in one or more exemplary embodiments of the present invention, the inner diameter of the annular bottom plate 123 can be 0.6 to 1.0 times the diameter of the inner cylinder 121, preferably 0.7 to 0.9 times.

[0052] like Figure 2 and Figure 3 As shown, the inlet diffuser 220 according to a specific embodiment of the present invention includes a sleeve composed of an inner cylinder 221 and an outer cylinder 222 coaxially arranged. The bottom end of the inner cylinder 221 is higher than the bottom end of the outer cylinder 222, and the area between the inner cylinder 221 and the outer cylinder 222 is a liquid holding area. An annular bottom plate 223 is coaxially connected to the bottom end of the outer cylinder 222, and a liquid phase channel is formed between the annular bottom plate 223 and the inner cylinder 221. Exemplarily, the outer periphery of the annular bottom plate 223 can be welded to the bottom end of the outer cylinder 222. A top cover 224 is provided above the inner cylinder 221, and a gas phase channel is formed between the top cover 224 and the inner cylinder 221. A rotating shaft 225 is coaxially inserted into the inner cylinder 221, and the lower end of the rotating shaft 225 passes through the annular bottom plate 223. A helical blade 226 is provided on the rotating shaft 225, and the helical blade 226 is disposed inside the inner cylinder 221 and drives the rotating shaft 225 to rotate. Two splash plates 227 are connected to the lower end of the rotating shaft 225. The splash plates 227 have a cone-shaped structure with the opening facing downwards.

[0053] Furthermore, in one or more exemplary embodiments of the present invention, the splash plate 227 may be composed of a plurality of fan-shaped pieces 2270 spaced apart, with each layer of the splash plate 227 having eight fan-shaped pieces 2270. Furthermore, in one or more exemplary embodiments of the present invention, the outer edge of the fan-shaped piece 2270 may extend with a horizontal segment 2271.

[0054] Furthermore, in one or more exemplary embodiments of the present invention, such as Figure 2 As shown, the cone angle of the upper splash plate 227 is greater than that of the lower splash plate 227.

[0055] Furthermore, in one or more exemplary embodiments of the present invention, such as Figure 3 As shown, the fan-shaped plates 2270 of the upper splash plate 227 and the fan-shaped plates 2270 of the lower splash plate 227 are arranged alternately. Further, in one or more exemplary embodiments of the present invention, the splash plate 227 is provided with a plurality of liquid-falling holes 2272. Further, in one or more exemplary embodiments of the present invention, the plurality of liquid-falling holes 2272 are distributed along concentric circles centered on the rotation axis 225.

[0056] The present invention will now be described in more detail by way of specific embodiments. It should be understood that the present invention is not limited thereto.

[0057] Example 1

[0058] In this embodiment, a super-large hydrogenation reactor with a diameter of 8m is provided with an inlet diffuser 120 according to the present invention at the feed inlet. (Reference) Figure 1 As shown, the inlet diffuser 120 is provided with a layer of helical blades 126 and a layer of conical splash plates 127. There are three helical blades 126. The cone angle of the conical splash plate 127 is 150°.

[0059] The original ultra-large hydrogenation reactor used a fixed inlet diffuser. After a period of commissioning, it was found that only under extremely harsh operating conditions could it produce qualified products, and its performance in coping with fluctuations in the material composition of the unit was extremely poor. After switching to the inlet diffuser of this embodiment, the operational stability of the unit was greatly improved.

[0060] Example 2

[0061] In this embodiment, the ultra-large hydrogenation reactor is equipped with the inlet diffuser 220 of the present invention, as shown in the reference. Figure 2 and Figure 3 As shown, the ultra-large hydrogenation reactor has a diameter of 8 m. The inlet diffuser 220 is equipped with one layer of helical blades 226 and two layers of conical splash plates 127. There are three helical blades 226. Each layer of conical splash plates 227 consists of eight fan-shaped blades 2270, with horizontal sections 2271 extending from the outer edge of the fan-shaped blades 2270. The cone angle of the upper layer of conical splash plates 227 is 120°, and the cone angle of the lower layer of conical splash plates 227 is 90°.

[0062] After using Example 1, the catalyst bed still has the problem of uneven radial temperature distribution. By further optimizing the inlet diffuser of the present invention, after using the inlet diffuser of Example 2, it can be found that the maximum radial temperature difference of the catalyst bed is reduced from the original 22.5℃ to 3.4℃ when comparing five temperature measuring points set at the same height.

[0063] The foregoing description of specific exemplary embodiments of the present invention is for illustrative and explanatory purposes. These descriptions are not intended to limit the invention to the precise forms disclosed, and it will be apparent that many changes and variations can be made in accordance with the foregoing teachings. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application, thereby enabling those skilled in the art to implement and utilize various different exemplary embodiments of the invention, as well as various different choices and variations. Any simple modifications, equivalent changes, and alterations made to the foregoing exemplary embodiments should fall within the scope of protection of the present invention.

Claims

1. An inlet diffuser, characterized in that, Liquid phase distribution in large-scale hydrogenation reactors includes: The sleeve consists of an inner cylinder and an outer cylinder arranged coaxially, with the bottom end of the inner cylinder higher than the bottom end of the outer cylinder, and the area between the inner cylinder and the outer cylinder is a liquid holding area; An annular bottom plate is coaxially connected to the bottom end of the outer cylinder, and a liquid phase channel is formed between the annular bottom plate and the inner cylinder. The area of ​​the liquid phase channel is less than or equal to the area of ​​the liquid holding area. A top cover is disposed above the inner cylinder, and a gas phase channel is formed between the top cover and the inner cylinder; A rotating shaft is coaxially inserted into the inner cylinder, and the lower end of the rotating shaft passes through the annular bottom plate. At least one layer of helical blades is disposed within the inner cylinder and drives the rotating shaft to rotate; and At least one splash plate, which has a downward-opening conical structure, is linked to the lower end of the rotating shaft; The gas phase enters the inner cylinder through the gas phase channel between the inner cylinder and the top cover. The forward-blowing spiral blades drive the rotating shaft to rotate, making full use of its kinetic energy when flowing in the inner cylinder, further driving the splash plate below the rotating shaft to rotate, thereby forming a stable centrifugal force field and providing the liquid phase with an initial horizontal velocity.

2. The inlet diffuser according to claim 1, characterized in that, The cone angle of each splash plate is 90~180°.

3. The inlet diffuser according to claim 1, characterized in that, Each splash plate consists of multiple fan-shaped plates spaced apart, with 3 to 8 fan-shaped plates per splash plate.

4. The inlet diffuser according to claim 3, characterized in that, The outer end of the fan-shaped piece is provided with serrations.

5. The inlet diffuser according to claim 3, characterized in that, The outer edge of the fan-shaped piece extends into a horizontal section.

6. The inlet diffuser according to claim 3, characterized in that, When two splash plates are provided, the fan-shaped blades of the upper splash plate and the fan-shaped blades of the lower splash plate are arranged alternately.

7. The inlet diffuser according to claim 1, characterized in that, When two splash plates are provided, the cone angle of the upper splash plate is greater than that of the lower splash plate.

8. The inlet diffuser according to claim 1, characterized in that, The splash plate is provided with multiple drop holes.

9. The inlet diffuser according to claim 8, characterized in that, The plurality of descending holes are distributed along concentric circles centered on the rotating shaft.

10. The inlet diffuser according to claim 1, characterized in that, The number of spiral blades in each layer is 3 to 5; the windward side of the spiral blades is in the axial direction, and the blade angle is 50 to 78°.

11. The inlet diffuser according to claim 1, characterized in that, The top cover is a conical, spherical, or flat structure.

12. The inlet diffuser according to claim 1, characterized in that, The inner cylinder is provided with a bearing bracket, and the rotating shaft is connected to the inner cylinder through the bearing bracket.

13. The inlet diffuser according to claim 1, characterized in that, The inner cylinder is provided with multiple upper support legs and multiple lower support legs. The inner cylinder is connected to the annular bottom plate through the lower support legs, and the top cover is connected to the upper end of the inner cylinder through the upper support legs.

14. The inlet diffuser according to claim 1, characterized in that, The inner diameter of the annular bottom plate is 0.6 to 1.0 times the diameter of the inner cylinder.

15. A hydrogenation reactor, characterized in that, include: The main body is a cylindrical structure, and a feed inlet is provided at the center of the upper end of the main body; as well as The inlet diffuser as described in any one of claims 1 to 14 is disposed at the feed inlet.

16. The hydrogenation reactor according to claim 15, characterized in that, The diameter of the body is greater than or equal to 6.5m.

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