Ultra-large hydrogenation reactor and its pre-dispensing components

Abstract

This invention discloses a pre-distribution assembly, comprising: an inlet diffuser, which includes: a sleeve, the bottom end of which is higher than the bottom end of the outer sleeve, with a liquid-holding zone between the inner and outer sleeves; an annular bottom plate coaxially connected to the bottom end of the outer sleeve, forming a liquid phase channel between the annular bottom plate and the inner sleeve; a top cover disposed above the inner sleeve, forming a gas phase channel between the top cover and the inner sleeve; a rotating shaft coaxially inserted into the inner sleeve, with its lower end passing through the annular bottom plate; at least one layer of helical blades disposed within the inner sleeve and driving the rotating shaft to rotate; and at least one layer of splash plates, which have a downward-opening conical structure, and are linked to the lower end of the rotating shaft; and a stepped distribution disk coaxially disposed below the inlet diffuser. This invention also discloses an ultra-large hydrogenation reactor. This invention, through the cooperation of the rotating inlet diffuser and the stepped distribution disk of the pre-distribution assembly, can achieve uniform distribution of gaseous and liquid phase materials within an ultra-large hydrogenation reactor.

Description

Technical Field

[0001] This invention relates to the field of hydrogenation reaction equipment technology, especially hydrogenation reaction equipment with large reactor scale, and particularly to an ultra-large hydrogenation reactor and its pre-dispensing components. 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, uses a hydrotreating catalyst to refine and crack the feedstock oil after it has been mixed with hydrogen in a specific ratio. The stability of the hydrotreating reaction within the reactor, the full effectiveness of the catalyst, and the achievement of high-quality products largely depend on the uniformity of the gas-liquid phase distribution within the catalyst bed. This uniformity is closely related to the design of the reactor's internal components. In short, the performance of these internal components directly affects catalyst lifespan, product quality, and the unit's operating cycle. Using high-performance internal components is tantamount to replacing the catalyst with a more active one. Therefore, research and engineering development of hydrotreating reactors and their internal components have been highly valued both domestically and internationally, with continuous updates to reactor internals aimed at achieving better results.

[0005] Hydrogenation reactors typically feed from the top center. 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 working conditions for the distribution plate. Patent document CN106268524A discloses a diffuser and a fixed-bed reactor. This diffuser is located at the inlet of the reactor body and includes a cylindrical body and swirl plates disposed within the cylindrical body. The top of the cylindrical body has a gas-liquid material inlet, and the bottom side has a gas-liquid material diffusion port. The swirl plates are curved panels extending axially along the cylindrical body to the gas-liquid material diffusion ports. Patent document CN205495530U discloses a swirling 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 cylindrical mixing chamber as a channel for the gas-liquid medium. It has the advantages of strong buffering effect, thorough gas-liquid mixing and large liquid phase spraying area. It can reduce the peak value of liquid phase radial distribution and uniformly diffuse the gas-liquid medium to the entire reactor cross section, creating conditions for the stable 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] Traditional hydrogenation reactors add a gas-liquid pre-distribution plate above the top distribution plate to improve the inlet conditions of the top distributor. Patent document CN109985573A discloses a hydrogenation reactor that improves liquid phase homogeneity. A folded-edge damping and equalization plate is installed in the unused space of the reactor head or at the upper end of the reactor shell. A chimney-type distributor vertically mounted on the tray distributes the material to the top distribution plate, providing a stable and uniform inlet condition, optimizing the material distribution in the top bed, and achieving the initial distribution function. Patent document CN204058374U discloses a fluid pre-distributor and a fluid pre-distribution plate. The fluid pre-distribution plate, installed above the gas-liquid distribution plate in a fixed-bed hydrogenation reactor, pre-distributes the hydrogenation feedstock, reducing the impact of the gas and liquid phases on the lower gas-liquid distribution plate, maintaining a stable liquid surface, and achieving a more uniform and effective distribution.

[0009] Existing technologies have not fundamentally solved the problem of gas-liquid two-phase distribution across the entire cross-section. While adding a gas-liquid pre-distribution plate avoids direct impact on the top distribution plate, the residual kinetic energy of the liquid material after passing through the inlet diffuser generates a strong inertial force, causing it to accumulate around the reactor after falling onto the top distribution plate. This typically results in a progressively increasing liquid layer distribution on the pre-distribution plate, meaning the liquid layer gradually rises from the center to the edges. As the processing scale of hydrogenation units increases, the diameter of hydrogenation reactors also gradually increases. In engineering implementation, it is clearly observed that the liquid layer height in the central region of the top distribution plate is relatively small, while the liquid layer height at the side walls is relatively large.

[0010] The distributors on the pre-distribution plate, which perform the distribution function, typically require a certain liquid level to activate before they begin operation. This means that when the distributors at the reactor sidewalls start up, the distributors in the center of the pre-distribution plate remain in standby mode due to insufficient liquid level, leading to a gradual increase in liquid level distribution on the top distribution plate. Even the best-performing distributors cannot achieve uniform material distribution under varying liquid levels, severely impacting the performance of the top distributor and inevitably increasing the radial temperature difference.

[0011] Secondly, influenced by the pressure distribution within the reactor head space, the gas phase tends to accumulate towards the center of the reactor after passing through the inlet diffuser, forming a distribution pattern completely opposite to that of the liquid phase. When the distributor in the center region of the pre-distribution disk fails to start properly, the gas phase can pass directly through the pre-distribution disk without mixing with the liquid phase, and in severe cases, it can even pass directly through the top distribution disk into the catalyst bed. As the diameter of the hydrogenation reactor increases, this leads to significant deviations in the distribution of gas and liquid phase materials.

[0012] Third, to ensure that the amount of liquid phase flowing through each distributor is the same and to achieve uniform coverage of the catalyst bed, the pre-distribution trays require extremely high levelness. However, as the diameter of hydrogenation reactors increases, trays are often installed in a modular assembly, making it impossible to accurately guarantee the overall levelness of the distribution plate surface. Installation errors typically cause the distribution plate surface to tilt by 1 / 8° to 1 / 2° in the horizontal direction, with a maximum tilt of 3 / 2°. Even if the initial levelness is high, it will lose its levelness during operation due to the combined effects of thermal expansion and material impact loads, thus affecting the distributor's performance.

[0013] 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

[0014] One of the objectives of this invention is to provide an ultra-large hydrogenation reactor and its pre-distribution components, thereby improving the problem of insufficient spraying area of ​​liquid phase materials in ultra-large hydrogenation reactors.

[0015] Another objective of this invention is to provide an ultra-large hydrogenation reactor and its pre-distribution assembly, thereby improving the problem of severe deviations in the distribution of gas and liquid phase materials on the top distribution plate of the hydrogenation reactor.

[0016] Another objective of this invention is to provide an ultra-large hydrogenation reactor and its pre-distribution components, thereby improving the problems of high installation accuracy requirements and easy deformation of the pre-distribution plate in existing hydrogenation reactors.

[0017] To achieve the above objectives, according to a first aspect of the present invention, a pre-dispensing assembly is provided, comprising: an inlet diffuser, including: a sleeve consisting of an inner cylinder and an outer cylinder coaxially arranged, 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; 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; and a stepped distribution disk coaxially disposed below the inlet diffuser, the stepped distribution disk having a stepped shape with a lower center and higher periphery.

[0018] Furthermore, in the above technical solution, the cone angle of each splash plate is 90 to 180°.

[0019] 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.

[0020] Furthermore, in the above technical solution, the outer end of the fan-shaped piece is provided with serrations.

[0021] 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.

[0022] 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.

[0023] 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°.

[0024] 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.

[0025] Furthermore, in the above technical solution, the top cover is a conical, spherical, or flat structure.

[0026] Furthermore, in the above technical solution, the stepped distribution tray includes: multiple trays, including a circular tray and multiple annular trays, the inner and outer diameters of the multiple trays are matched sequentially, and they are distributed in a multi-layer stepped manner with the circular tray as the center, the circular tray being the lowest layer and the annular tray with the largest outer diameter being the highest layer, and each of the multiple trays is provided with multiple sieve holes; and a connector, which connects two adjacent trays and seals the interlayer gap between the two adjacent trays.

[0027] Furthermore, in the above technical solution, each annular tray is composed of multiple tray plates spliced ​​together.

[0028] According to a second aspect of the present invention, the present invention provides an ultra-large hydrogenation reactor, comprising: a body having a cylindrical structure and a feed inlet at the center of the upper end of the body; a pre-distribution component as described in any of the above technical solutions, wherein an inlet diffuser is disposed at the feed inlet; and a top distribution plate disposed below the stepped distribution plate.

[0029] Furthermore, in the above technical solution, a ring of bosses is provided on the inner wall of the main body, and the outer periphery of the stepped distribution plate is installed in the main body through the bosses.

[0030] Furthermore, in the above technical solution, the boss is welded inside the upper head of the body.

[0031] Furthermore, in the above technical solution, the diameter of the main body is greater than or equal to 6.5m.

[0032] Compared with the prior art, the present invention has one or more of the following beneficial effects:

[0033] 1. The pre-distribution component of the present invention, through the cooperation of the inlet diffuser and the stepped distribution plate, can achieve uniform distribution of gas-liquid phase materials in an ultra-large hydrogenation reactor.

[0034] 2. The rotary inlet diffuser of this invention is a movable internal component, enabling the distribution of the liquid phase within the ultra-large hydrogenation reactor after being sprayed out through a small-diameter pipe. The gas phase, through the channel of the inner cylinder, is driven by the forward-blowing helical blades to rotate the main shaft, fully utilizing its kinetic energy during flow within the pipe. This further drives the splash plate below the main shaft to rotate, thereby forming a stable centrifugal force field and providing the liquid phase with an initial horizontal velocity. The liquid phase flows out from the center of the annular bottom plate, acquiring different initial horizontal velocities as it passes through different positions of the splash plate serrations or the gaps between adjacent fan-shaped blades before entering the reactor. This allows the spray area to cover the entire reactor cross-section, meeting the requirements for liquid phase coverage area in large-scale equipment.

[0035] 3. The rotary inlet diffuser of the present invention is suitable for materials with a large gas content. It can achieve long-term stable operation while ensuring a stable gas phase material flow rate. When the liquid phase flow rate decreases, that is, when the liquid phase feed rate is at a low point, the spray range can still remain stable and will not shrink towards the center of the reactor. This can create stable working conditions for the top distribution plate and has a strong adaptability to fluctuations in the liquid phase material flow rate.

[0036] 4. The spiral blades of the rotary inlet diffuser of this invention are located inside the inner cylinder. During operation, the power primarily comes from the large amount of kinetic energy generated by the gas flow. This energy is first converted into mechanical energy from 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 leads to rapid attenuation of the accumulated energy of the gas phase after entering the reactor, preventing the liquid phase from receiving continuous propulsion from the gas phase.

[0037] 5. The stepped distribution tray of the present invention forms a multi-layered stepped distribution through circular trays and multiple annular trays, which changes the arrangement of traditional pre-distribution trays. By creating a discontinuity between adjacent trays, it ensures that the liquid layers on each tray are not on the same horizontal plane, reducing the obstruction effect of liquids flowing in the same direction during the flow process and preventing the liquid phase from accumulating around the reactor. The liquid layers on adjacent trays do not directly contact each other, and there is no single continuous liquid surface covering the entire cross-section of the reactor. This fundamentally breaks the "bridging" effect caused by the mutual dependence between liquid phases and eliminates the phenomenon of liquid layer incremental distribution from the center to the edge.

[0038] 6. The stepped distribution plate of the present invention does not have a conventional gas-liquid distributor. The liquid phase flows down through the sieve holes on each layer of the tray. The amount of liquid phase passing through each sieve hole is basically the same, ensuring that the gas partial pressure is roughly the same at all points of the reactor cross section, achieving uniform distribution of the gas phase, avoiding large deviations in the gas and liquid phase materials, and providing good prerequisites for the stable operation of the hydrogenation unit.

[0039] 7. In this invention, the trays in the stepped distribution tray are at different horizontal positions, which effectively reduces the cumulative error in the radial direction. During installation, it is only necessary to ensure the levelness of the trays within the same layer, without needing to accurately ensure the overall levelness of the stepped distribution tray, thereby reducing the installation difficulty.

[0040] 8. Each tray can be divided into multiple tray plates according to the manhole size. The number of tray plates and tray layers increases accordingly with the increase of the diameter of the hydrogenation reactor, which improves the resistance of the unit to thermal expansion and material impact loads during operation.

[0041] 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

[0042] Figure 1 This is a partial structural schematic diagram of an ultra-large hydrogenation reactor according to an embodiment of the present invention.

[0043] Figure 2 This is a schematic diagram of the structure of an inlet diffuser according to an embodiment of the present invention.

[0044] Figure 3 This is a top view of the splash plate according to an embodiment of the present invention.

[0045] Figure 4 This is a bottom view of the stepped distribution plate according to an embodiment of the present invention.

[0046] Explanation of key figure labels:

[0047] 100 - Ultra-large hydrogenation reactor, 110 - Body, 111 - Feed inlet, 112 - Boss, 120 - Inlet diffuser, 121 - Inner cylinder, 1211 - Lower support leg, 1212 - Upper support leg, 1213 - Bearing bracket, 122 - Outer cylinder, 123 - Annular bottom plate, 124 - Top cover, 125 - Rotating shaft, 126 - Spiral blade, 127 - Splash plate, 1270 - Fan-shaped plate, 130 - Stepped distribution plate, 131 - Circular tray, 132 - Annular tray, 133 - I-beam, 134 - Support beam. Detailed Implementation

[0048] 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.

[0049] 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.

[0050] 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.

[0051] 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.

[0052] like Figure 1 As shown, the ultra-large hydrogenation reactor 100 according to a specific embodiment of the present invention has a cylindrical body 110, and a feed inlet 111 is provided at the center of the upper end of the body 110. An inlet diffuser 120 is provided at the feed inlet 111, and a stepped distribution plate 130, a top distribution plate, and a catalyst bed (not shown in the figure) are arranged sequentially from top to bottom below the inlet diffuser 120.

[0053] Furthermore, in one or more exemplary embodiments of the present invention, a ring of bosses 112 is provided on the inner wall of the body 110, and the outer periphery of the stepped distribution disk 130 is mounted inside the body 110 via the bosses 112. Furthermore, in one or more exemplary embodiments of the present invention, the bosses 112 are welded to the upper end cap of the body 110. It should be understood that the bosses 112 may also not be provided inside the upper end cap.

[0054] Combination Figures 1 to 4As shown, the pre-dispensing assembly according to a specific embodiment of the present invention includes an inlet diffuser 120 and a stepped dispensing disk 130. The inlet diffuser 120 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. 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. The rotating shaft 125 is provided with at least one layer of spiral blades 126, which are disposed inside the inner cylinder 121 and drive the rotating shaft 125 to rotate. At least one layer of splash plate 127 is linked to the lower end of the rotating shaft 125, and the splash plate 127 has a cone-shaped structure with its opening facing downward. The stepped distribution plate 130 is coaxially disposed below the inlet diffuser 120, and the stepped distribution plate 130 has a stepped shape with a lower center and a higher periphery.

[0055] Furthermore, in one or more exemplary embodiments of the present invention, the top cover 124 may be a conical, spherical, or flat structure. For example, as shown... Figure 1 As shown, the top cover 124 has a flat plate structure with the edges turned up and having toothed grooves.

[0056] 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.

[0057] 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.

[0058] Further, in one or more exemplary embodiments of the present invention, the cone angle of each splash plate 127 can be 90° to 180°. Further, in one or more exemplary embodiments of the present invention, each splash plate 127 can be composed of a plurality of fan-shaped blades 1270 spaced apart, with the number of fan-shaped blades in each splash plate 127 being 3 to 8. Further, in one or more exemplary embodiments of the present invention, the outer ends of the fan-shaped blades 1270 are provided with serrations. Further, in one or more exemplary embodiments of the present invention, two splash plates are provided, with the fan-shaped blades 1270 of the upper splash plate and the fan-shaped blades 1270 of the lower splash plate arranged alternately. Further, in one or more exemplary embodiments of the present invention, two splash plates are provided, with the cone angle of the upper splash plate being larger than that of the lower splash plate.

[0059] Furthermore, in one or more exemplary embodiments of the present invention, the number of each layer of spiral blades 126 may be 3 to 5.

[0060] Furthermore, in one or more exemplary embodiments of the present invention, the inner diameter of the annular bottom plate 123 is 0.6 to 1.0 times the diameter of the inner cylinder 121, preferably 0.7 to 0.9 times.

[0061] Furthermore, in one or more exemplary embodiments of the present invention, the stepped distribution tray 130 includes multiple trays, one of which is a circular tray 131, and the others are annular trays 132. The inner and outer diameters of the multiple trays are matched sequentially, and they are distributed in multiple stepped layers with the circular tray 131 as the center, wherein the circular tray 131 is the lowest layer, and the annular tray 132 with the largest outer diameter is the highest layer. Both the circular tray 131 and the multiple annular trays 132 are provided with multiple sieve holes (not shown in the figure). Adjacent trays are connected by connectors, and the connectors seal the interlayer gaps between adjacent trays.

[0062] Furthermore, in one or more exemplary embodiments of the present invention, adjacent trays are connected by I-beams 133. In the two adjacent trays, the inner edge of the upper tray overlaps the upper surface of the upper flange of the I-beam 133, and the outer edge of the lower tray overlaps the upper surface of the lower flange of the I-beam 133. The web of the I-beam 133 seals the interlayer gap between the two adjacent trays. Exemplarily, the I-beam 133 is a ring beam, and adjacent I-beams 133 (ring beams) are connected by a plurality of radially arranged support beams 134 to form an integral mounting frame. The distribution of the support beams 134 and the ring beams can be as follows: Figure 4 As shown, the present invention is not limited thereto. Furthermore, in one or more exemplary embodiments of the present invention, the height difference between two adjacent trays is approximately 200–400 mm, i.e., the height of the I-beam.

[0063] refer to Figure 1 In one or more exemplary embodiments of the present invention, the pre-distribution component operates as follows: the gas-liquid mixture falls from the inlet 111 of the ultra-large hydrogenation reactor 100 onto the top cover 124 above the inner cylinder 121 of the inlet diffuser 120. After being buffered by the folded edge, most of the liquid phase enters the liquid-holding area between the outer cylinder 122 and the inner cylinder 121 along the circumferential grooves. The liquid phase material passes through the liquid phase channel between the lower end of the inner cylinder 121 and the annular bottom plate 123, and falls sequentially onto the upper splash plate 127 and the lower splash plate 127 under the action of gravity. At the same time, a certain liquid layer is formed on the annular bottom plate 123, preventing the gas phase material from entering the ultra-large hydrogenation reactor 100 along the same path.

[0064] Since the inner diameter of the annular bottom plate 123 is 0.7 to 0.9 times the diameter of the inner cylinder 121, a liquid seal is formed when the liquid phase flows through the liquid phase channel. Affected by this, the gaseous material can only pass through the gas phase channel between the upper end of the inner cylinder 121 and the top cover 124, and then flow downwards along the center of the inner cylinder 121. Simultaneously, the forward-blowing spiral blades 126 drive the rotating shaft 125 to rotate, which in turn drives the two layers of splash plates 127 at the lower end of the rotating shaft 125 to rotate. After the material passes through the inlet diffuser 120, the time it takes to fall onto the lower distribution plate is mainly affected by gravity, while the distribution across the reactor cross-section is affected by the initial horizontal velocity. That is, the greater the initial horizontal velocity of the liquid phase, the larger the spray area it can cover. According to the circular motion formula, when the angular velocity of the splash plate is determined, the linear velocity of its edge is only related to the diameter. The inlet diffuser 120 of this invention ensures that the material leaves the splash plate at different positions by multi-stage diversion of the liquid phase, utilizing the difference in its initial velocity to form a distribution along the entire reactor cross-section.

[0065] The splash plate 127 can be composed of multiple fan-shaped plates 1270 spaced apart, with the blank areas of adjacent splash plates 127 alternating. Therefore, when the liquid phase falls onto the upper splash plate 127, it is split. Some material falls along the blank area of ​​the upper splash plate 127 onto the lower splash plate 127, while another part falls along the upper splash plate 127 onto the blank area of ​​the lower splash plate 127. Some material falls directly into the reactor through the gap between the two splash plates 127. The liquid phase sliding down the splash plate 127, due to the centrifugal force field generated by the rotation, acquires a certain initial horizontal velocity, the magnitude of which is related to its distance from the rotation axis 125. The outer edges of both splash plates 127 are serrated, which allows the liquid phase detaching from the edge of the splash plate 127 to create a velocity boundary, further enhancing the liquid phase splitting effect and achieving full coverage of the entire reactor cross-section, meeting the trend of large-scale hydrogenation units.

[0066] The spiral blade 126 is located inside the inner cylinder 121, in a position where the gas phase has significant kinetic energy. Therefore, after establishing a stable liquid level, it enters normal working condition, effectively converting its accumulated energy into the mechanical energy of the splash plate 127. After the splash plate 127 collides with the liquid phase, it converts some of the mechanical energy into the kinetic energy of the liquid phase moving horizontally, completing a continuous energy transfer process. In this process, the vertical kinetic energy of the gas phase is converted into the horizontal kinetic energy of the liquid phase via the rotating shaft. Although some losses occur, this process still has positive significance in terms of the rational utilization of energy.

[0067] After most of the liquid material falls onto the stepped distribution tray 130, it first accumulates along the inner wall of the main body 110. Under the influence of gravity, the liquid layer tends to flow towards the center. Some of the liquid phase falls into the top distribution tray through the sieve holes on the annular tray 132, while the remaining liquid phase flows through the annular tray 132. Since the adjacent trays are arranged in a stepped manner along the axial direction, the liquid phases on each tray are not on the same horizontal plane, and there is no direct contact between the liquid layers. The remaining liquid phase is obstructed by the inner wall of the main body 110 or the web of the I-beam 133, and can only flow inward through the artificially created fault to reach the lower tray.

[0068] Furthermore, in one or more exemplary embodiments of the present invention, each annular tray 132 may be composed of multiple tray plates joined together. The tray plates may be divided according to the size of the manhole.

[0069] Furthermore, in one or more exemplary embodiments of the present invention, the diameter of the body 110 is greater than or equal to 6.5m.

[0070] 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.

[0071] Example 1

[0072] In this embodiment, reference Figures 1-4 As shown, the ultra-large hydrogenation reactor 100 is equipped with the pre-distribution components of this invention, namely, an inlet diffuser 120 and a stepped distribution plate 130. The ultra-large hydrogenation reactor 100 has a diameter of 6.8 m. The inlet diffuser 120 has two layers of spiral blades 126 and two layers of conical splash plates 127. Each layer of spiral blades has three blades, and each layer of splash plates consists of three fan-shaped blades. The fan-shaped blades of the upper and lower layers of splash plates are arranged alternately. The cone angle of the upper splash plate is 150°, and the cone angle of the lower splash plate is 120°. The structure of the stepped distribution plate 130 is as described above, wherein the annular tray 132 is divided into multiple tray plates according to the manhole size. The connecting component is an I-beam 133, which is a ring beam. Adjacent ring beams are connected by a support beam 134. In this embodiment, the hydrogenation reactor 100 body 110 has a ring of bosses 112.

[0073] During installation, the mounting frame consisting of the I-beam 133 (ring beam) and the support beam 134 is fixed inside the body 110 of the hydrogenation reactor 100. Multiple tray plates of each layer of annular trays 132 and circular trays 131 are then connected and installed to the ring beam. The height difference between two adjacent tray layers is approximately 220 mm.

[0074] The liquid phase is sprayed onto the edge of the hydrogenation reactor 100 through the inlet diffuser 120, achieving full coverage of the material along the entire reactor cross-section. The stepped distribution plate 130 reduces the distribution deviation of the gas and liquid phases, providing friendly, stable, and uniform inlet conditions for the top distribution plate. Compared with conventional inlet diffusers and pre-distribution plates, the pre-distribution component of this embodiment solves the problem of localized temperature runaway and abnormal pressure drop during unit operation. By comparing temperature measuring points set at the same height, it can be found that the maximum radial temperature difference of the catalyst bed is reduced from 14.2℃ to 1.2℃, and the pressure drop is reduced from 220kPa to 65kPa.

[0075] 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. A pre-allocation component, characterized in that, include: Inlet diffuser, comprising: 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; 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, having an opening-down conical structure, is linked to the lower end of the rotating shaft; and A stepped distribution plate, coaxially positioned below the inlet diffuser, is shaped like a stepped structure with a lower center and higher periphery. The stepped distribution plate includes multiple trays, comprising a circular tray and multiple annular trays. The inner and outer diameters of the multiple trays are sequentially matched and arranged in a multi-layered stepped distribution centered on the circular tray. The circular tray is the lowest layer, and the annular tray with the largest outer diameter is the highest layer. Each of the multiple trays is provided with multiple sieve holes. A connector connects two adjacent tray layers and seals the interlayer gap between adjacent tray layers.

2. The pre-allocation component according to claim 1, characterized in that, The cone angle of each splash plate is 90~180°.

3. The pre-allocation component 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 pre-allocation component according to claim 3, characterized in that, The outer end of the fan-shaped piece is provided with serrations.

5. The pre-allocation component 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.

6. The pre-allocation component according to claim 5, 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.

7. The pre-allocation component 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°.

8. The pre-allocation component according to claim 1, characterized in that, The inner diameter of the annular bottom plate is 0.7 to 0.9 times the diameter of the inner cylinder.

9. The pre-allocation component according to claim 1, characterized in that, The top cover is a conical, spherical, or flat structure.

10. The pre-allocation component according to claim 1, characterized in that, Each of the aforementioned annular trays is composed of multiple tray plates joined together.

11. A super-large 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; The pre-dispensing component as described in any one of claims 1 to 10, wherein the inlet diffuser is disposed at the feed inlet; and A top dispensing tray is located below the stepped dispensing tray.

12. The ultra-large hydrogenation reactor according to claim 11, characterized in that, A ring of protrusions is provided on the inner wall of the main body, and the outer periphery of the stepped distribution plate is installed in the main body through the protrusions.

13. The ultra-large hydrogenation reactor according to claim 12, characterized in that, The boss is welded inside the upper end cap of the body.

14. The ultra-large hydrogenation reactor according to claim 11, characterized in that, The diameter of the body is greater than or equal to 6.5m.

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