A homogeneous gas-liquid distribution suspended bed reactor for heavy oil hydrogenation

Abstract

This invention relates to the field of reactor technology and discloses a uniform gas-liquid distribution suspended bed reactor for heavy oil hydrogenation, comprising a reactor shell; a gas-liquid distribution plate is horizontally arranged at the lower end of the inner cavity of the reactor shell, and a Venturi annular gas-liquid diffuser is arranged on the gas-liquid distribution plate, with a pre-distribution chamber formed at the bottom of the gas-liquid distribution plate; the Venturi annular gas-liquid diffuser includes an external gas conduit that penetrates the gas-liquid distribution plate. The Venturi annular gas-liquid diffuser of this invention, through the synergistic action of the liquid phase flow annular nozzle and the gas phase flow annular nozzle, enables the high-speed ejected liquid phase to actively shear and break up the low-speed gas phase, generating a uniform cluster of small bubbles. This greatly increases the gas-liquid contact area, significantly improves the dissolution rate and mass transfer efficiency of hydrogen into heavy oil, thereby directly improving the hydrogenation reaction depth and product quality, while also effectively protecting the catalyst in the catalyst suspended bed reaction zone.

Description

Technical Field

[0001] This invention relates to the field of reactor technology, and more particularly to a uniform gas-liquid distribution suspended bed reactor for heavy oil hydrogenation. Background Technology

[0002] In the field of heavy oil hydrotreating, to avoid the inherent defects of downward trickle bed reactors, which are prone to coking and blockage due to the fixed catalyst bed, upward bubbling bed or suspended bed reactors are widely used in industry. In these reactors, the gas and liquid phases flow upward from the bottom, and the catalyst particles are in a suspended or slightly fluidized state. However, the composition of heavy oil feedstock is complex, containing impurities such as gums, asphaltenes, and solid particles. To prevent blockage of the distributor channels, the channel diameter of the distribution element is usually designed to be large. This results in the low-density gas phase (hydrogen) having weak injection kinetic energy. After entering the high-density liquid phase, it quickly floats to the surface under the action of buoyancy and agglomerates with each other, making it difficult to form a uniformly dispersed group of small bubbles.

[0003] In existing technologies, the flow pattern dominated by large bubbles directly leads to poor gas-liquid distribution within the bed: large bubbles concentrate and rise in local channels, generating violent throttling disturbances that scour surrounding catalyst particles at high speed, which is the main cause of catalyst mechanical damage; at the same time, insufficient gas supply in many areas results in a small mass transfer contact area between hydrogen and fuel, restricting the improvement of hydrogenation reaction depth and product quality; furthermore, this non-uniform flow state weakens the heat transfer and mixing efficiency inside the reactor; uneven bubble distribution directly leads to uneven spatial distribution of reaction heat, making it difficult for reaction heat to be removed in a timely and uniform manner, forming a significant temperature gradient within the bed. This temperature unevenness not only causes local overheating and accelerates thermal cracking and coking, but also the concentration gradient caused by insufficient mixing further affects the selectivity of the reaction and the overall operational stability. Summary of the Invention

[0004] The technical problem to be solved by this invention is that in the prior art, the large bubbles generated by the diffuser lead to uneven gas-liquid distribution, which in turn causes catalyst breakage and low mass transfer efficiency. At the same time, the lack of efficient heat transport and mixing means inside the reactor results in a significant temperature gradient and mixing dead zone in the bed, which exacerbates the risk of coking and affects the stability of the reaction. To address this, we propose a uniform gas-liquid distribution suspended bed reactor for heavy oil hydrogenation.

[0005] To achieve the above objectives, this application adopts the following technical solution: a uniform gas-liquid distribution suspended bed reactor for heavy oil hydrogenation, comprising a reactor shell, a gas-liquid outlet disposed at the top of the reactor shell, a gas-liquid inlet disposed at the bottom of the reactor shell, and a cooling structure disposed on the inner periphery of the reactor shell.

[0006] A gas-liquid distribution plate is horizontally arranged at the lower end of the inner cavity of the reactor shell. A Venturi annular gas-liquid diffuser is arranged on the gas-liquid distribution plate. A pre-distribution chamber is formed at the bottom of the gas-liquid distribution plate, and a catalyst suspension bed reaction zone is formed at the top. The upper end of the pre-distribution chamber is a gas phase space, and the lower end is a liquid phase space.

[0007] The Venturi annular gas-liquid diffuser includes an outer gas conduit that runs through the gas-liquid distribution plate. The lower end of the outer gas conduit corresponds to the gas phase space. An inner liquid conduit is coaxially arranged inside the outer gas conduit. The lower end of the inner liquid conduit extends to the liquid phase space, and the upper end extends to the top of the outer gas conduit and is provided with a bell mouth. A gas phase flow annular nozzle is formed between the bottom of the bell mouth and the top of the outer gas conduit. A horizontal circular plate is provided above the bell mouth. A liquid phase flow annular nozzle is formed between the bottom of the horizontal circular plate and the top of the bell mouth.

[0008] Preferably, a connecting column is installed at the upper end of the external gas conduit, the flared end is installed on the connecting column, the horizontal circular plate is movably sleeved on the connecting column, a bimetallic composite circular plate corresponding to the horizontal circular plate is installed at the top of the connecting column, and the bottom of the bimetallic composite circular plate is connected to the horizontal circular plate through a connecting block. The bimetallic composite circular plate is configured to bend towards the flared end when the temperature rises, thereby causing the horizontal circular plate to move downward to reduce the gap of the liquid phase flow annular nozzle.

[0009] Preferably, the bimetallic composite circular plate is formed by combining two nickel-based alloy layers.

[0010] Preferably, hollow diffusion cones are provided on the outer side of the horizontal circular plate and the upper end of the external gas duct, with the two hollow diffusion cones arranged opposite each other.

[0011] Preferably, the catalyst suspension bed reaction zone is provided with a thermosiphon assembly, which includes a vertically arranged outer cylinder with both ends closed. The inner side of the outer cylinder is filled with a phase change working fluid, and an inner cylinder is installed inside the outer cylinder. The lower end of the thermosiphon assembly is an evaporation section, and the upper end is a condensation section, which is used to transfer the heat of reaction through the phase change cycle of the internal phase change working fluid.

[0012] Preferably, the phase change working medium is sodium or a sodium-potassium alloy.

[0013] Preferably, a heat-conducting ring is provided at the upper end of the catalyst suspension bed reaction zone, the upper end of the outer cylinder is mounted on the heat-conducting ring, a heat-conducting rod corresponding to the outer cylinder is vertically mounted on the heat-conducting ring, and the lower end of the heat-conducting rod is connected to the bimetallic composite circular plate.

[0014] Preferably, the lower outer wall of the outer cylinder is provided with a protruding structure for enhancing heat transfer and inducing slurry flow.

[0015] Preferably, the protruding structure is an axial fin, a helical fin, or a discrete convex shaft.

[0016] Preferably, the sidewall of the heat-conducting ring is provided with a connector for connecting to the cooling structure, and the connector is a heat-conducting structure or a non-heat-conducting structure.

[0017] The technical effects and advantages of this invention are as follows:

[0018] In this invention, a Venturi annular gas-liquid diffuser solves the core problem of uneven gas-liquid distribution caused by traditional large-diameter nozzles. This Venturi annular gas-liquid diffuser utilizes gravity pre-separation to ensure that gas and liquid enter independent flow channels. Then, through the synergistic effect of the liquid-phase flow annular nozzle and the gas-phase flow annular nozzle, the high-speed ejected liquid phase actively shears and breaks up the low-speed gas phase, generating a uniform cluster of small bubbles. This greatly increases the gas-liquid contact area, significantly improving the dissolution rate and mass transfer efficiency of hydrogen into heavy oil, thereby directly improving the depth of the hydrogenation reaction and product quality. It also effectively protects the catalyst in the catalyst suspension bed reaction zone. Based on the above, the bimetallic composite circular plate, in conjunction with a movable horizontal circular plate, allows for passive and real-time fine-tuning of the gap of the liquid-phase flow annular nozzle according to the reaction state. The system achieves dynamic optimization of gas-liquid distribution. When the slurry temperature rises in a localized area, it indicates that the reaction at that point is exothermic or that poor flow is causing heat accumulation. As a result, the bimetallic composite disc bends towards the flared end due to the heat, which in turn causes the horizontal disc to move downward. This automatically reduces the gap of the liquid phase flow annular nozzle. The reduced gap increases the liquid jet velocity and enhances the shearing effect on the gas phase, thereby generating finer and denser bubble clusters at that point. This increases the gas-liquid contact area and significantly improves the hydrogen mass transfer rate in that hot spot area. Moreover, the high-speed liquid flow and the refined bubbles together enhance the heat removal in that area, forming a self-regulating cycle that promotes cooling by enhancing mass transfer and thus inhibits further temperature rise. This mechanism enables the reactor to autonomously smooth out microscale temperature fluctuations caused by uneven flow or reaction.

[0019] In this invention, the thermosiphon assembly utilizes the rapid circulation of the internal phase change working fluid—absorbing heat and boiling in the evaporation section and releasing heat and condensing in the condensation section—to directly transfer the heat concentrated in the lower reaction zone to the upper space. This effectively flattens the axial temperature distribution, suppresses local overheating, and simultaneously forms an upward thermal buoyancy plume. This plume, together with the backflow from the cooler region, constitutes an organized natural circulation. The raised structure on the outer wall of the evaporation section alters the local flow path and momentum distribution, converting some axial momentum into tangential and radial components, inducing swirling flow and a stable upward channel. This significantly enhances gas-liquid mixing and heat uniformity. Furthermore, with the connecting parts, the condensation section of the thermosiphon assembly can be selectively thermally connected to or non-thermally isolated from the inner wall cooling structure, allowing for flexible configuration to prioritize radial cooling or axial temperature uniformity. Attached Figure Description

[0020] The disclosure of this invention is illustrated with reference to the accompanying drawings. It should be understood that the drawings are for illustrative purposes only and are not intended to limit the scope of protection of this invention. In the drawings, the same reference numerals are used to refer to the same parts:

[0021] Figure 1 This is a schematic diagram of the structure of the present invention;

[0022] Figure 2 This is a schematic diagram of the internal structure of the present invention;

[0023] Figure 3 This is a schematic diagram of the overall structure of the outer cylinder and gas-liquid distribution plate of the present invention;

[0024] Figure 4 For the present invention Figure 3 A structural diagram from the bottom perspective;

[0025] Figure 5 This is a schematic diagram of the Venturi annular gas-liquid diffuser of the present invention;

[0026] Figure 6 This is a schematic diagram of the Venturi annular gas-liquid diffuser of the present invention from another perspective;

[0027] Figure 7 This is a cross-sectional structural diagram of the Venturi annular gas-liquid diffuser of the present invention in use.

[0028] Figure 8 This is a schematic diagram of the exploded structure of the Venturi annular gas-liquid diffuser of the present invention;

[0029] Figure 9 This is a schematic diagram of the overall structure of the outer cylinder and the heat-conducting ring of the present invention;

[0030] Figure 10 This is a schematic cross-sectional view of the thermosiphon assembly of the present invention;

[0031] Figure 11 This is a schematic diagram of the structure of the present invention in the state of the protrusion structure and the outer cylinder in conjunction.

[0032] Legend: 1. Reactor shell; 2. Gas-liquid outlet; 3. Gas-liquid inlet; 4. Gas-liquid separator; 5. Gas outlet; 6. Liquid outlet; 7. Cooling coil; 8. Heat dissipation casing; 9. Gas-liquid distribution plate; 10. Heat-conducting ring; 11. Outer cylinder; 12. Heat-conducting rod; 13. Connector; 14. Hollow diffuser cone; 15. Outer gas conduit; 16. Inner liquid conduit; 17. Bimetallic composite circular plate; 18. Horizontal circular plate; 19. Bell mouth; 20. Connecting column; 21. Gas phase space; 22. Liquid phase space; 23. Liquid phase flow annular nozzle; 24. Gas phase flow annular nozzle; 25. Inner cylinder; 26. Through hole; 27. Protruding structure; 28. Connecting block. Detailed Implementation

[0033] It is readily understood that, based on the technical solution of this invention, those skilled in the art can propose various interchangeable structural methods and implementations without altering the essential spirit of the invention. Therefore, the following detailed embodiments and accompanying drawings are merely illustrative examples of the technical solution of this invention and should not be considered as the entirety of the invention or as limitations or restrictions on the technical solution of this invention.

[0034] Reference Figures 1-11As shown, a uniform gas-liquid distribution suspended bed reactor for heavy oil hydrogenation includes a reactor shell 1, a gas-liquid outlet 2 located at the top of the reactor shell 1, a gas-liquid inlet 3 located at the bottom of the reactor shell 1, and a cooling structure located on the inner periphery of the reactor shell 1. The cooling structure includes a heat dissipation sleeve 8 installed on the inner wall of the reactor shell 1. Cooling coils 7 for circulating cooling medium are arranged inside the heat dissipation sleeve 8, and both ends of the cooling coils 7 extend to the outside of the reactor shell 1. The cooling medium is circulated by pumping to cool the heat generated during the operation of the reactor shell 1. The gas-liquid outlet 2 is located away from the reactor. A gas-liquid separator 4 is provided at one end of the shell 1. The upper end of the gas-liquid separator 4 has a gas outlet 5, and the lower end has a liquid outlet 6. Gas and liquid discharged from the gas-liquid outlet 2 enter the gas-liquid separator 4. The gas can be discharged and collected through the gas outlet 5, and the liquid can be discharged and upgraded through the liquid outlet 6. A gas-liquid distribution plate 9 is horizontally arranged at the lower end of the inner cavity of the reactor shell 1. A Venturi annular gas-liquid diffuser is provided on the gas-liquid distribution plate 9. A pre-distribution chamber is formed at the bottom of the gas-liquid distribution plate 9, and a catalyst suspension bed reaction zone is formed at the top. The upper end of the pre-distribution chamber is a gas phase space 21, and the lower end is a liquid phase space 22. As a preferred embodiment, the Venturi annular diffuser... The gas-liquid diffuser includes multiple external gas conduits 15 that are disposed through the gas-liquid distribution plate 9 and arranged in an array. The lower end of each external gas conduit 15 corresponds to the gas phase space 21. An inner liquid conduit 16 is coaxially disposed inside the external gas conduit 15. The lower end of the inner liquid conduit 16 extends to the liquid phase space 22, and the upper end extends to the top of the external gas conduit 15 and is provided with a bell mouth 19. A gas phase flow annular nozzle 24 is formed between the bottom of the bell mouth 19 and the top of the external gas conduit 15. A horizontal circular plate 18 is disposed above the bell mouth 19, and the diameter of the horizontal circular plate 18 is adapted to the outer diameter of the bell mouth 19. A liquid flow annular nozzle 23 is formed between the bottom of the horizontal circular plate 18 and the top of the flared mouth 19. In order to connect the inner liquid conduit 16, the outer gas conduit 15 and the horizontal circular plate 18 into one unit, multiple connecting columns 20 are installed at the upper end of the outer gas conduit 15. The outer periphery of the flared mouth 19 at the upper end of the inner liquid conduit 16 is installed on the connecting columns 20. The horizontal circular plate 18 is also installed on the connecting columns 20. At the same time, in order to guide the diffusion of liquid phase and bubbles, hollow diffusion cones 14 are respectively provided on the outer side of the horizontal circular plate 18 and the upper end of the outer gas conduit 15. The two hollow diffusion cones 14 are arranged opposite each other, and the opposite sides form a guiding slope.By employing a Venturi annular gas-liquid diffuser, the core problem of uneven gas-liquid distribution caused by traditional large-diameter nozzles is solved. This Venturi annular gas-liquid diffuser utilizes gravity pre-separation to ensure that gas and liquid enter independent flow channels respectively. Then, through the synergistic action of the liquid-phase flow annular nozzle 23 and the gas-phase flow annular nozzle 24, the high-speed ejected liquid phase actively shears and breaks up the low-speed gas phase, generating a uniform cluster of small bubbles. This significantly increases the gas-liquid contact area, substantially improving the dissolution rate and mass transfer efficiency of hydrogen into heavy oil, thereby directly improving the hydrogenation reaction depth and product quality. It also effectively protects the catalyst in the catalyst suspension bed reaction zone. Due to the small size and uniform distribution of the bubbles, the large bubble channels with localized spurs are eliminated, and the fluid disturbance within the catalyst suspension bed reaction zone becomes gentle and uniform, greatly reducing the problem of mechanical breakage of catalyst particles caused by severe scouring, laying the foundation for long-term stable operation of the reactor.

[0035] Furthermore, in order to change the gap of the liquid flow annular nozzle 23 when the temperature rises, a horizontal circular plate 18 is vertically and movably fitted onto the outside of the connecting column 20. A bimetallic composite circular plate 17 corresponding to the horizontal circular plate 18 is installed on the top of the connecting column 20. The periphery of the bimetallic composite circular plate 17 is fixed to multiple connecting columns 20. The bottom of the bimetallic composite circular plate 17 is connected to the horizontal circular plate 18 through a connecting block 28. The bimetallic composite circular plate 17 is configured to bend towards the flared end 19 when the temperature rises, thereby causing the horizontal circular plate 18 to move downward to reduce the gap of the liquid flow annular nozzle 23. The upper and lower layers of the bimetallic composite circular plate 17 are both made of nickel-based alloys resistant to high temperature and high pressure hydrogen corrosion. The upper layer uses Inconel 625 or Inconel 718 nickel-based alloys with a low coefficient of thermal expansion, and the lower layer uses Incoloy 800H or Alloy with a high coefficient of thermal expansion. The 617 grade nickel-based alloy, through the combination of a bimetallic composite circular plate 17 and a movable horizontal circular plate 18, can passively and in real-time fine-tune the gap of the liquid phase flow annular nozzle 23 according to the reaction state, thereby achieving dynamic optimization of gas-liquid distribution. Specifically, when the slurry temperature in a certain local area rises, it indicates that the reaction exotherm is enhanced or the flow is obstructed, leading to heat accumulation. The bimetallic composite circular plate 17 is therefore heated and bends towards the flared end 19, thereby driving the horizontal circular plate 18 downward through the connecting block 28, automatically reducing the gap of the liquid phase flow annular nozzle 23. The reduced gap increases the liquid jet velocity and enhances the shearing effect on the gas phase, thereby generating finer and denser bubble clusters at that point, increasing the gas-liquid contact area, significantly improving the hydrogen mass transfer rate in the hot spot area. Moreover, the high-speed liquid flow and the refined bubbles together enhance the heat removal in this local area, forming an autonomous regulation cycle that promotes cooling by enhancing mass transfer and thus inhibits further temperature rise. This mechanism enables the reactor to autonomously smooth out microscale temperature fluctuations caused by uneven flow or reaction.

[0036] The catalyst suspension bed reaction zone is equipped with a thermosiphon assembly, which includes multiple vertically arranged outer cylinders 11, both ends of which are closed. The inner sides of the outer cylinders 11 and inner cylinders 25 are evacuated and filled with a phase change working fluid. The inner cylinder 25 is installed inside the outer cylinders 11, and the lower and upper sidewalls of the inner cylinder 25 are evaporation sections and condensation sections, respectively. This is used to transfer the heat of reaction through the phase change cycle of the internal phase change working fluid. The phase change working fluid is preferably sodium or a sodium-potassium alloy to adapt to long-term operation in high-temperature environments. The materials of the outer cylinders 11 and inner cylinders 25 are preferably Incoloy 800H, Alloy 617, or Inconel. Alloy materials of grade 625 are used to meet the requirements of high-temperature and high-pressure hydrogen environments. In order to increase the heat exchange surface area and enhance the heat transfer efficiency between the thermosiphon tube and the slurry, and at the same time, by disturbing and guiding the fluid, a swirling or upward flow that promotes uniform mixing of the slurry is induced in the reactor. A protruding structure 27 is provided on the lower outer wall of the outer cylinder 11 to enhance heat transfer and induce slurry flow. The protruding structure 27 is preferably an axial fin, a spiral fin, or a discrete convex shaft. Through the thermosiphon assembly, the heat concentrated in the lower reaction zone can be directly transferred to the upper space by utilizing the rapid circulation of the internal phase change working fluid, which absorbs heat and boils in the evaporation section and releases heat and condenses in the condensation section. This effectively flattens the axial temperature distribution, suppresses local overheating, and forms an upward thermal buoyancy plume. It forms an organized natural circulation with the backflow in the cooler area. The protruding structure 27 on the outer wall of the evaporation section can change the local flow channel and momentum distribution, converting part of the axial momentum into tangential and radial components, inducing swirling flow and a stable upward channel, and significantly enhancing gas-liquid mixing and heat distribution.

[0037] A heat-conducting ring 10 is provided at the upper end of the catalyst suspension bed reaction zone, and the upper end of the outer cylinder 11 is mounted on the heat-conducting ring 10. The side wall of the heat-conducting ring 10 is provided with a connector 13 for connecting to the cooling structure. The connector 13 can be a heat-conducting structure or a non-heat-conducting structure. When the connector 13 is a heat-conducting structure, its end away from the heat-conducting ring 10 is fixed to the inner wall of the heat dissipation sleeve 8. It is preferably made of Inconel 600 / 625 / 617, which can quickly guide heat to the cooling structure and reduce the radial temperature gradient. At the same time, expansion compensation can be provided on the connector 13 to relieve thermal stress. When the connector 13 is a non-heat-conducting structure, a metal material with a low thermal conductivity can be selected. At the same time, the connection with the heat dissipation sleeve 8 can be insulated with ceramic fiber or alumina gaskets, so that the heat is mainly released to the surrounding slurry, enhancing natural circulation and reducing the axial temperature difference. By selectively connecting the condensation section of the thermosiphon assembly to the inner wall cooling structure in a heat-conducting manner or isolating it in a non-heat-conducting manner, it can be flexibly configured to prioritize radial cooling or axial temperature uniformity respectively.

[0038] In addition, a heat-conducting rod 12 corresponding to the outer cylinder 11 is vertically installed on the heat-conducting ring 10. The lower end of the heat-conducting rod 12 is connected to the bimetallic composite circular plate 17. It can be connected to the outer fixed area of ​​the bimetallic composite circular plate 17 or to the middle area of ​​the bimetallic composite circular plate 17. If it is connected to the middle area, the lower end of the heat-conducting rod 12 needs to be set as a telescopic structure to accommodate the vertical deformation of the bimetallic composite circular plate 17. After the bimetallic composite circular plate 17 is thermally connected to the condensation section of the thermosiphon assembly through the heat-conducting rod 12, its adjustment logic is upgraded from a single local response to a local and overall coordinated mode. The temperature of the condensation section of the thermosiphon assembly directly reflects the intensity of heat transport in that area, that is, the overall heat load level. While sensing the local slurry temperature, the heat-conducting rod 12 and the bimetallic composite circular plate 17 also receive the regional heat load signal that represents the future thermal trend. When the reactor faces global changes such as a change in feed properties that lead to an increase in the overall reaction heat release rate, the enhanced heat flux will first cause the temperature of the condensation section of the thermosiphon component to rise, thereby driving the bimetallic composite circular plate 17 to reduce the gap of the liquid phase flow annular nozzle 23 in advance. This allows the gas-liquid dispersion and mass transfer efficiency of the entire reactor cross section to be improved in advance before the overall temperature rises significantly. This forward-looking adjustment enables the system to actively match the increased reaction heat load and prevent the formation of a large-scale temperature gradient by uniformly distributing and enhancing mass transfer, thereby improving the stability of the system from passively bearing to actively maintaining it.

[0039] Working Principle: Heavy oil and hydrogen enter the pre-distribution chamber through the gas-liquid inlet 3 at the bottom of the reactor shell 1. After initial separation under gravity, the gas phase, due to its lower density, resides in the gas phase space 21, while the liquid phase resides in the liquid phase space 22. They then enter the reaction zone through independent channels of the Venturi annular gas-liquid diffuser: the liquid phase rises from the inner liquid conduit 16 immersed in the liquid phase space 22, while the gas phase enters through the annular gap between the top of the outer gas conduit 15 and the inner liquid conduit 16. At the top of the Venturi annular gas-liquid diffuser, the liquid phase is ejected at high speed through the liquid phase flow annular nozzle 23. The high flow rate is due to the greater density of the liquid phase flow, resulting in greater inertial force and a greater ability to overcome liquid resistance, thus extending the injection distance. The gas phase flows at high speed from the gas phase flow annular nozzle 24 at the upper end of the outer gas conduit 15. Upon ejection, the gas stream is rapidly decelerated upon encountering the liquid space. This is because the lower the density of the gas phase flow, the weaker its inertial force. Combined with buoyancy, its ability to overcome liquid resistance is weak, resulting in a very short ejection distance. However, due to its location in the negative pressure region below the high-speed liquid flow, the gas phase flow is drawn into the high-speed liquid flow by the attraction of buoyancy and the negative pressure region generated by the liquid flow. This causes strong shearing of the gas phase flow, breaking it into uniform microbubbles. These small bubbles have low buoyancy and easily move horizontally in the liquid, thus achieving the goal of uniformly diffusing the gas phase flow into the liquid flow. This achieves a high degree of gas-liquid dispersion and uniform distribution at the source, effectively avoiding the problems of catalyst scouring and breakage and insufficient mass transfer area caused by large bubbles. The slurry carrying the fine bubbles then enters the catalyst suspension upwards. In the floating bed reaction zone, hydrogenation occurs and heat is released. Simultaneously, an array of thermosiphon components distributed within the bed operates. Its evaporation section absorbs the reaction heat, causing the internal phase-change working fluid to undergo a phase change, rapidly transferring the heat to the condensation section. This process directly and efficiently transfers the reaction heat, significantly reducing the axial temperature gradient. During this process, a cooling medium circulates in the cooling coil 7, cooling the interior through the heat dissipation sleeve 8. Furthermore, the connector 13 is connected to the inner wall of the heat dissipation sleeve 8. When the connector 13 is a thermally conductive structure, it can also transfer heat to the heat dissipation sleeve 8, thereby reducing the radial temperature gradient and forming an upward thermal buoyancy plume. This, along with the backflow from the cooler area, constitutes an organized natural circulation. Combined with the protruding structure 27 on the outer wall of the evaporation section, it can alter the local flow path and momentum. The distribution process converts a portion of the axial momentum into tangential and radial components, inducing swirling flow and a stable upward channel, significantly enhancing gas-liquid mixing and heat distribution. Simultaneously, the bimetallic composite circular plate 17 adjusts the gap of the liquid flow annular nozzle 23 according to its local temperature, performing self-optimization. Furthermore, through the thermally conductive connection between the heat-conducting rod 12 and the condensation section of the thermosiphon assembly, the bimetallic composite circular plate 17 can detect heat flow signals characterizing changes in the overall heat load of the region in advance. When changes in feed lead to increased exothermic reactions, the liquid flow annular nozzle 23 can reduce its gap to pre-enhance the global mass transfer intensity to match the increased heat load. Finally, the reacted gas-liquid mixture rises to the top of the reactor and is discharged from the gas-liquid outlet 2 into the gas-liquid separator 4, and then the liquid is discharged from the liquid outlet 6.The gas is discharged from gas outlet 5, thus completing a highly efficient, uniform, stable, and adaptive heavy oil hydrogenation reaction process.

[0040] The technical scope of this invention is not limited to the content described above. Those skilled in the art can make various modifications and variations to the above embodiments without departing from the technical concept of this invention, and all such modifications and variations should fall within the protection scope of this invention.

Claims

1. A uniform gas-liquid distribution suspended bed reactor for hydroprocessing of heavy oil, characterized in that, The reactor shell comprises a reactor shell, a gas-liquid outlet arranged at the top end of the reactor shell, a gas-liquid inlet arranged at the bottom of the reactor shell, and a cooling structure arranged on the inner side of the reactor shell; The lower end of the inner cavity of the reactor shell is horizontally provided with a gas-liquid distribution disc, the gas-liquid distribution disc is provided with a Venturi annular gas-liquid diffuser, the bottom of the gas-liquid distribution disc forms a pre-distribution chamber, the top of the gas-liquid distribution disc forms a catalyst suspension bed reaction zone, the upper end of the pre-distribution chamber is a gas phase space, and the lower end of the pre-distribution chamber is a liquid phase space; The Venturi annular gas-liquid diffuser comprises an outer gas conduit arranged through the gas-liquid distribution disc, the lower end of the outer gas conduit corresponds to the gas phase space, the inner side of the outer gas conduit is coaxially provided with an inner liquid conduit, the lower end of the inner liquid conduit extends to the liquid phase space, and the upper end of the inner liquid conduit extends to the top of the outer gas conduit and is provided with a bell mouth, the bottom of the bell mouth and the top of the outer gas conduit form a gas phase flow annular nozzle, a horizontal circular plate is arranged above the bell mouth, and the bottom of the horizontal circular plate and the top of the bell mouth form a liquid phase flow annular nozzle; The catalyst suspension bed reaction zone is provided with a thermosyphon assembly, the thermosyphon assembly comprises a vertical outer cylinder, the two ends of the outer cylinder are closed, the inner side of the outer cylinder is filled with a phase change working medium, and an inner cylinder is mounted on the inner side of the outer cylinder, the lower end of the thermosyphon assembly is an evaporation section, the upper end of the thermosyphon assembly is a condensation section, and the thermosyphon assembly is used for transferring reaction heat through phase change circulation of the internal phase change working medium; The upper end of the catalyst suspension bed reaction zone is provided with a heat conduction ring, and the upper end of the outer cylinder is mounted on the heat conduction ring; The lower end of the outer cylinder is provided with a protruding structure on the outer wall for strengthening heat transfer and inducing slurry flow; The side wall of the heat conduction ring is provided with a connecting piece for connecting with the cooling structure, and the connecting piece is a heat conduction structure or a non-heat conduction structure.

2. The uniform gas-liquid distribution suspended bed reactor for heavy oil hydrogenation according to claim 1, characterized in that: The upper end of the outer gas conduit is mounted with a connecting column body, the bell mouth is mounted on the connecting column body, the horizontal circular plate is movably sleeved on the connecting column body, the top of the connecting column body is mounted with a bimetallic composite circular plate corresponding to the horizontal circular plate, the bottom of the bimetallic composite circular plate is connected with the horizontal circular plate through a connecting block, and the bimetallic composite circular plate is configured to bend towards the bell mouth when the temperature rises, thereby driving the horizontal circular plate to move downwards to reduce the gap of the liquid phase flow annular nozzle.

3. The uniform gas-liquid distribution suspended bed reactor for heavy oil hydroprocessing of claim 2, wherein: The bimetallic composite circular plate is formed by two layers of nickel-based alloy.

4. The uniform gas-liquid distribution suspended bed reactor for heavy oil hydroprocessing of claim 2, wherein: The outer side of the horizontal circular plate and the upper end of the outer gas conduit are respectively provided with hollow diffusion cones, and the two hollow diffusion cones are oppositely arranged.

5. The uniform gas-liquid distribution suspended bed reactor for heavy oil hydroprocessing of claim 2, wherein: The phase change working medium is sodium or sodium-potassium alloy.

6. The uniform gas-liquid distribution suspended bed reactor for heavy oil hydroprocessing of claim 2, wherein: A heat conduction rod corresponding to the outer cylinder is vertically mounted on the heat conduction ring, and the lower end of the heat conduction rod is connected with the bimetallic composite circular plate.

7. The uniform gas-liquid distribution suspended bed reactor for heavy oil hydroprocessing of claim 2, wherein: The protruding structure is an axial fin or a spiral fin or a discrete convex shaft.

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