Gas-liquid distributor and hydrogenation reactor using the same

Abstract

The application discloses a gas-liquid distributor and a hydrogenation reactor using the same. The gas-liquid distributor comprises a main pipe body which is arranged vertically and fixed on a gas-liquid distribution disc of the hydrogenation reactor; a gas phase inlet is arranged on the top side wall of the main pipe body and uniformly distributed along the circumference of the main pipe body, and the gas phase flows from top to bottom along the axial direction in the main pipe body; a liquid phase overflow hole is arranged above the gas-liquid distribution disc and uniformly distributed along the circumference of the main pipe body; the liquid phase overflow hole comprises a first overflow hole which is always open and a second overflow hole which is selectively opened and closed by the pressure difference between the inside and outside of the main pipe body; the liquid phase enters the main pipe body along the radial direction; and a flow breaker is arranged at the bottom of the main pipe body and used for pulverizing and atomizing the liquid phase. The application can effectively solve the problem of uneven gas-liquid distribution under the conditions of large gas-liquid phase load and large liquid level fluctuation; and has the advantages of simple structure, small pressure drop, large operation flexibility, good gas-liquid mixing effect and strong anti-installation inclination performance.

Description

Technical Field

[0001] This invention relates to the field of petroleum refining and chemical equipment technology, and particularly to a gas-liquid distributor and a hydrogenation reactor using the distributor. Background Technology

[0002] The gas-liquid distributor is a crucial internal component in a hydrogenation reactor. Its main function is to improve the flow pattern of the gas-liquid two-phase fluid, ensuring that the incoming gas-liquid reactants are evenly distributed on the bed surface, thereby achieving sufficient contact between the gas-liquid mixture and the catalyst. Since hydrogenation is an exothermic reaction, uneven material distribution can cause significant radial temperature differences within the catalyst bed. Localized overheating of the bed can affect catalyst activity and even lead to catalyst deactivation due to coking. Therefore, the effectiveness of the gas-liquid distributor directly impacts whether the catalyst can fully exert its hydrogenation performance and whether the hydrogenation reactor can achieve optimal production efficiency.

[0003] Existing gas-liquid distributors for fixed-bed hydrogenation reactors can be classified into three types according to the liquid phase entry method: overflow type, suction type, and a combination of both. Overflow type gas-liquid distributors mostly adopt a main tube structure, where the liquid accumulates to a certain height on the distribution plate and then directly enters the main tube through the overflow hole. This type of gas-liquid distributor has advantages such as simple structure, low pressure drop, small size and installation space, low central confluence, and strong scale-holding capacity. However, it has poor resistance to installation tilting, is prone to wall flow, and its gas-liquid mixing effect and droplet atomization performance are not as good as suction type gas-liquid distributors.

[0004] Suction-type gas-liquid distributors typically have a bubble-cap structure. The lower end of the bubble cap has a number of evenly distributed slits. High-speed gaseous material entering through these slits creates a strong suction effect within the annular space between the bubble cap and the main pipe, causing the liquid to break up into droplets. These droplets then follow the rising airflow into the main pipe for gas-liquid mixing and distribution. This type of gas-liquid distributor has advantages such as strong resistance to installation tilt, good gas-liquid mixing effect, and good droplet atomization performance. However, its structure is relatively complex, its pressure drop is large, and it exhibits a noticeable "central confluence" phenomenon.

[0005] The inventors discovered through research that the distribution performance of a gas-liquid distributor is mainly reflected in three aspects: first, the integrity of the liquid spray surface, which is usually related to the size of the liquid spray surface at the distributor outlet and the number of liquid phase distribution points flowing from the distributor per unit area to the catalyst bed; second, the uniformity of the liquid spray surface, which is reflected in the difference in the amount of liquid sprayed at different locations on the catalyst bed; and third, operational flexibility, i.e., the ability to maintain normal operation when the gas-liquid load fluctuates significantly. When designing a gas-liquid distributor, factors such as droplet atomization performance, pressure drop, resistance to installation tilt, and scale tolerance also need to be considered. For gas-liquid distributors where some or all of the liquid phase enters the main pipe via overflow, to reduce the impact of liquid level fluctuations on distribution performance, it is common practice to open holes at different heights in the main pipe or to install the gas-liquid distributor at different heights. When the liquid level just submerges the upper overflow hole, the hydraulic pressure of the liquid phase above the upper overflow hole cannot provide sufficient inflow velocity for the liquid phase, preventing the liquid phase entering the main pipe from colliding well with the gas inside the pipe, resulting in wall flow and affecting the gas-liquid mixing effect. Under certain special operating conditions, if the liquid level accumulates too high, some of the liquid phase will enter the main pipe through the gas phase inlet, causing poor gas-liquid mixing and even "pipe overflow" phenomenon, resulting in the failure of the gas-liquid distributor.

[0006] 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

[0007] The purpose of this invention is to provide a gas-liquid distributor and a hydrogenation reactor using the distributor, which can effectively solve the problem of uneven gas-liquid distribution under conditions of large fluctuations in gas-liquid phase load and liquid level height; it has the advantages of simple structure, low pressure drop, large operational flexibility, good gas-liquid mixing effect and strong resistance to installation tilt.

[0008] Another objective of this invention is to effectively solve the "overflowing" phenomenon caused by excessive liquid accumulation around the gas-liquid distributor.

[0009] To achieve the above objectives, according to a first aspect of the present invention, a gas-liquid distributor is provided for use in a hydrogenation reactor, comprising: a main pipe, which is a vertically arranged tubular structure and fixed on a gas-liquid distribution plate of the hydrogenation reactor; a gas phase inlet, which is disposed on the top sidewall of the main pipe and uniformly distributed along the circumference of the main pipe, wherein the gas phase flows axially from top to bottom within the main pipe; a liquid phase overflow orifice, which is disposed above the gas-liquid distribution plate and uniformly distributed along the circumference of the main pipe; the liquid phase overflow orifice includes a normally open first overflow orifice and a second overflow orifice that is selectively opened and closed by means of a pressure difference between the inside and outside of the main pipe; the liquid phase enters the main pipe radially; and a flow-breaking plate, which is disposed at the bottom of the main pipe for pulverizing and atomizing the liquid phase.

[0010] Furthermore, in the above technical solution, the selective opening and closing of the second overflow orifice can be controlled by a first opening and closing unit, which may include: a ring magnet, which is fixedly disposed on the outer wall of the main pipe at the corresponding position of the second overflow orifice, the inner diameter of the ring magnet being equal to or slightly larger than the diameter of the second overflow orifice; and a cover plate, which is disposed on the inner wall of the main pipe at the corresponding position of the second overflow orifice. When the gas phase load in the main pipe is lower than the threshold, the combined effect of the pressure difference and hydraulic force inside and outside the main pipe is less than the magnetic force of the ring magnet on the cover plate, and the cover plate is in a closed state. When the gas phase load in the main pipe is higher than the threshold, the combined effect of the pressure difference and hydraulic force inside and outside the main pipe is greater than the magnetic force of the ring magnet on the cover plate, and the cover plate is in an open state.

[0011] Furthermore, in the above technical solution, the cover plate may include: a connecting part, which is fixedly disposed above the second overflow hole on the inner wall of the main pipe; and a cover plate body, which seals and covers the second overflow hole and can be pivotally connected to the connecting part.

[0012] Furthermore, in the above technical solution, multiple serrated sections can be evenly arranged at the bottom of the cover plate body.

[0013] Furthermore, in the above technical solution, the liquid phase overflow hole may also include a third overflow hole that can be selectively opened and closed, and the third overflow hole may be positioned higher than the first overflow hole and the second overflow hole.

[0014] Furthermore, in the above technical solution, the selective opening and closing of the third overflow orifice can be controlled by a second opening and closing unit, which includes: a float ball, the height of which is lower than the height of the gas phase inlet; a connecting rod, the upper end of which is fixed to the bottom of the float ball and the lower end of which is fixed to the sealing plate; and a sealing plate, which seals and covers the outside of the third overflow orifice under normal operating conditions. When the liquid accumulation height on the outside of the main pipe exceeds the height of the float ball, the float ball drives the sealing plate to move upward through the connecting rod and opens the third overflow orifice.

[0015] Furthermore, in the above technical solution, the float can be set on the fixed groove and the connecting rod is inserted through the perforation on the fixed groove to achieve the float's positioning.

[0016] Furthermore, in the above technical solution, the fixing groove can be designed as an arc and fixedly installed on the outer wall of the main body near the gas phase inlet, and liquid flow holes can be evenly arranged on the surface of the fixing groove.

[0017] Furthermore, in the above technical solution, the flow disruptor can be fixed to the bottom of the main pipe by a support member. The flow disruptor can be designed as a solid circular plate with serrated sections around its outer circumference, which spray the gas-liquid mixture.

[0018] Furthermore, in the above technical solution, the top of the main body may be provided with a top cover, which may be a conical panel, and the outer edge of the conical panel may protrude from the outer side wall of the main body.

[0019] Furthermore, in the above technical solution, the shape of the gas phase inlet can be an inverted triangle.

[0020] According to a second aspect of the present invention, a hydrogenation reactor is provided, comprising a gas-liquid distributor as described in any one of the preceding claims, wherein the gas-liquid distributors are a plurality of such distributors and are evenly arranged and fixedly installed on a gas-liquid distribution plate within the hydrogenation reactor.

[0021] Furthermore, in the above technical solution, the spacing between the gas-liquid distributors can be smaller than the diameter of the spray surface formed by the gas-liquid mixture on the catalyst bed.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] 1) The gas-liquid distributor of this invention can dynamically regulate the liquid inlet flow rate to achieve a balance between the gas inlet flow rate and the liquid inlet flow rate, and has the advantages of high operational flexibility and uniform gas-liquid distribution. The gas phase flows at high speed in the main pipe with a small inner diameter, thereby creating a pressure difference between the inside and outside of the gas-liquid distributor. This pressure difference provides the main driving force for the liquid phase to flow into the main pipe through the overflow hole, while the hydraulic pressure of the liquid phase above the overflow hole due to the static liquid height provides a secondary driving force. When the gas phase load is small, the combined effect of the pressure difference and hydraulic force inside and outside the gas-liquid distributor is less than the magnetic force of the annular magnet on the cover plate. The cover plate closes, the second overflow orifice is closed, and the flow rate of liquid phase overflowing into the main pipe is limited, which is beneficial for the liquid phase to accumulate at a higher level on the gas-liquid distribution plate. Under the action of the two driving forces, the liquid phase enters the main pipe at high speed through the normally open first overflow orifice. The high-speed gas phase generates shear force on the liquid phase, causing it to be cut and broken, thus achieving a better gas-liquid mixing effect. When the gas phase load is large, the combined effect of the pressure difference and hydraulic force inside and outside the gas-liquid distributor is greater than the magnetic force of the annular magnet on the cover plate. The cover plate opens, and the flow rate of liquid phase overflowing into the main pipe increases. By dynamically adjusting the liquid inlet flow rate, the liquid inlet flow rate and the gas inlet flow rate are always kept in a basic balance, which is more conducive to gas-liquid mixing. In addition, the degree of cover plate opening changes with the gas phase load, which allows for dynamic control of the liquid inlet flow rate, which helps to increase the uniformity of gas-liquid distribution and improves the operational flexibility of the distributor.

[0024] 2) The gas-liquid distributor of the present invention has strong anti-tilt performance. Since the pressure difference between the inside and outside of the gas-liquid distributor is the main driving force for the liquid phase to flow into the main pipe, the hydraulic pressure of the liquid phase above the overflow hole due to the static liquid height is only a secondary driving force, and the main driving force is much greater than the secondary driving force. Therefore, the influence of the static liquid height change on the liquid phase flow rate overflowing into the main pipe is effectively reduced. The cover plate and the ring magnet are designed to help the liquid phase accumulate a certain liquid level above the overflow hole, ensuring that the flow rate of the liquid phase entering the main pipe is relatively consistent.

[0025] 3) The gas-liquid distributor of the present invention can effectively avoid the occurrence of "pipe overflow" phenomenon and can still maintain normal operation when the liquid level is too high. The float, connecting rod and sealing slide plate can allow the liquid phase to enter the main pipe through the third overflow hole when the liquid level is too high, preventing the liquid phase from flowing into the gas phase inlet and affecting the gas-liquid distribution effect;

[0026] 4) The design of the fixed tank in this invention can not only support and limit the float, but also has a certain scale-holding capacity. Some liquid phase flows through the fixed tank and flows to the gas-liquid distribution plate below through the liquid flow hole opened on the fixed tank, avoiding the liquid phase directly impacting the distribution plate. Some solid dirt can be deposited at the bottom of the fixed part.

[0027] 5) Under the influence of a large internal and external pressure difference in the gas-liquid distributor, the liquid phase is radially ejected from the normally open first overflow hole at a high horizontal velocity, colliding perpendicularly with the axially downward gas phase, resulting in excellent liquid phase atomization and breaking effect. When the cover plate is open and the second overflow hole is used, the liquid phase first impacts the cover plate, which is beneficial for liquid phase atomization. A portion of the liquid phase flows along the plane of the cover plate to its lower end, and the serrations at the lower end of the cover plate facilitate liquid phase atomization and breaking. Therefore, using the gas-liquid distributor of this invention, even under large gas phase load fluctuations, good liquid phase atomization can still be achieved.

[0028] 6) The gas-liquid distributor of the present invention has the advantages of simple structure, low pressure drop, and good gas-liquid mixing effect and droplet atomization performance. The liquid phase mainly enters the main body through overflow, reducing the pressure drop caused by the gas phase carrying the liquid phase into the main body. The flow-breaking plate at the lower end of the main body expands the liquid phase spraying area of ​​the gas-liquid distributor. By setting the interval between adjacent gas-liquid distributors to be smaller than the diameter of the spray surface formed by the gas-liquid mixture on the catalyst bed, the spray surfaces of multiple gas-liquid distributors are superimposed, increasing the integrity and uniformity of the liquid spray surface. The gas-liquid mixture can be more completely and uniformly distributed to the catalyst bed, improving the catalyst utilization rate and helping to reduce the peak value of the liquid phase along the radial distribution. On the other hand, it helps the liquid phase to be broken into small droplets due to collision, further enhancing the gas-liquid mixing effect and droplet atomization performance.

[0029] 7) The top cover design of the gas-liquid distributor of the present invention can effectively prevent the gas and liquid phases from directly entering the main pipe body from top to bottom, thus affecting the gas-liquid mixing effect; on the other hand, it can reduce the impact of the liquid phase on the gas-liquid distribution plate, so that the liquid phase forms a stable liquid level on the distribution plate.

[0030] 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

[0031] Figure 1 This is a first cross-sectional schematic diagram of the gas-liquid distributor of the present invention (showing a first overflow orifice, a second overflow orifice, and a first opening and closing unit for controlling the opening and closing of the second overflow orifice).

[0032] Figure 2 This is a schematic diagram of the structure of the second overflow hole cover plate of the present invention.

[0033] Figure 3 This is a schematic diagram of the open state of the second overflow hole cover plate of the present invention.

[0034] Figure 4This is a second cross-sectional schematic diagram of the gas-liquid distributor of the present invention (showing the third overflow orifice and the second opening and closing unit for controlling the opening and closing of the third overflow orifice).

[0035] Figure 5 This is a schematic diagram of the open state of the sealing slide plate of the third overflow hole of the present invention.

[0036] Figure 6 This is a schematic diagram of the float fixing groove of the present invention.

[0037] Figure 7 This is a schematic diagram of the structure of the flow-breaking plate of the present invention.

[0038] Explanation of key figure labels:

[0039] 1-Main body, 10-Top cover, 11-Gas inlet, 12-Liquid overflow hole, 12A-First overflow hole, 12B-Second overflow hole, 12C-Third overflow hole, 2-Gas-liquid distribution plate, 3-Annular magnet, 4-Cover plate, 41-Connecting part, 42-Cover plate body, 43-Serrated part, 5-Flow breaking plate, 50-Toothed part, 51-Supporting component, 6-Sealing slide plate, 7-Connecting rod, 8-Float ball, 81-Fixing groove, 810-Liquid flow hole. Detailed Implementation

[0040] 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.

[0041] 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.

[0042] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “upper,” 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.

[0043] 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.

[0044] The gas-liquid distributor of this invention can control the opening degree of the cover plate according to the magnitude of the gas phase load, under the combined action of the pressure difference force and magnetic force inside and outside the main pipe, to achieve dynamic regulation of the liquid inlet. It also provides a good breaking effect on the liquid, ensuring thorough mixing and uniform distribution of the gas-liquid medium onto the catalyst bed. Furthermore, this invention effectively avoids the "overflow" phenomenon, maintaining normal operation of the distributor even when the liquid level outside the main pipe is too high. This gas-liquid distributor can be used in various trickle-flow fixed-bed hydrogenation reactors, such as petroleum hydrocarbon hydrogenation processes.

[0045] Example 1

[0046] like Figure 1 As shown, Embodiment 1 of the present invention provides a gas-liquid distributor applicable to a hydrogenation reactor. It includes a main pipe 1, which is a vertically arranged tube structure fixed to a gas-liquid distribution plate 2 on the hydrogenation reactor (not shown in the figure). The sidewall of the main pipe 1 is provided with a gas inlet 11 and a liquid overflow hole 12, and a flow-breaking plate 5 is provided at the bottom. The gas inlet 11 is located on the top sidewall of the main pipe 1 and is evenly distributed along the circumference of the main pipe, allowing the gas phase to flow axially from top to bottom within the main pipe. The liquid overflow hole 12 is located on the lower sidewall of the main pipe 1, above the gas-liquid distribution plate 2, and is evenly distributed along the circumference of the main pipe. The liquid overflow hole 12 includes a normally open first overflow hole 12A and a second overflow hole 12B that is selectively opened and closed according to the pressure difference between the inside and outside of the main pipe. Through the liquid overflow hole 12, the liquid phase can enter the main pipe 1 radially. The flow-breaking plate 5 is located at the bottom of the main pipe 1 and is used to atomize and pulverize the liquid phase. Furthermore, the top of the main pipe 1 is provided with a top cover 10, which can be a conical panel. The outer edge of the conical panel preferably protrudes from the outer side wall of the main pipe. The top cover 10 is fixedly connected to the top of the main pipe. On the one hand, it can effectively prevent the gas-liquid two-phase fluid flowing in from above from directly entering the main pipe. On the other hand, it can reduce the impact of the liquid phase on the gas-liquid distribution plate 2. The protruding conical panel can guide the liquid phase to the gas-liquid distribution plate 2.

[0047] Specifically, the gas phase inlet 11 can be an inverted triangle (see reference). Figure 1 The design, with a larger upper opening and a smaller lower opening, allows for better introduction of the gas phase into the main pipe 1, ensuring smooth axial downward movement of the gas phase within the main pipe 1. The gas phase inlet 11 can also be rectangular, circular, or a combination of both. The number of gas phase inlets and the opening area can be designed and adjusted according to changes in process conditions.

[0048] Furthermore, in this invention, the liquid phase mainly enters the main pipe body through overflow, reducing the pressure drop caused by the gas phase carrying the liquid phase into the main pipe body. The gas phase enters from the top of the main pipe body 1 and moves downward along the axial direction, while the liquid phase enters radially from the lower part of the main pipe body 1. The flow directions of the gas and liquid phases are basically perpendicular. The high-speed gas phase generates shear force on the liquid phase, causing the liquid phase to be cut and broken, thereby achieving a better gas-liquid mixing effect. The inventors have found that most gas-liquid distributors used in the prior art only have normally open overflow holes and the overflow holes are set at different heights. However, this setting makes it difficult for the gas-liquid distributor to maintain normal operation when the gas-liquid load fluctuates greatly. In view of this, this invention sets the overflow holes to be partially open and partially selectively open or close according to different gas-liquid load states, thereby realizing dynamic adjustment of the liquid phase flow rate. Therefore, this invention provides a normally open first overflow hole 12A and a selectively openable and closeable second overflow hole 12B. The selective opening and closing of the second overflow hole is controlled by a first opening and closing unit, further as follows: Figure 1 As shown, the first opening and closing unit may include an annular magnet 3 and a cover plate 4. The annular magnet 3 is fixedly disposed on the outer wall of the main pipe at the corresponding position of the second overflow hole 12B. The inner diameter of the annular magnet 3 is equal to or slightly larger than the diameter of the second overflow hole 12B, allowing the liquid phase to pass smoothly. The cover plate 4 is disposed on the inner wall of the main pipe at the corresponding position of the second overflow hole 12B. When the gas phase load in the main pipe 1 is lower than a certain threshold (this threshold can be obtained according to process conditions and experiments), the combined effect of the pressure difference and hydraulic force inside and outside the main pipe is less than the magnetic force of the annular magnet 3 on the cover plate 4, and the cover plate is in a closed state. When the gas phase load in the main pipe 1 is higher than this threshold, the combined effect of the pressure difference and hydraulic force inside and outside the main pipe is greater than the magnetic force of the annular magnet 3 on the cover plate 4. At this time, the cover plate 4 is opened, allowing the liquid phase outside the pipe to enter the main pipe through the second overflow hole 12B. It should be noted here that the inventors discovered that by designing the inner diameter of the main pipe 1 to be relatively small, the gas phase can flow at high speed within the main pipe, thereby creating a large pressure difference between the inside and outside of the gas-liquid distributor. This pressure difference provides the primary driving force for the liquid phase to flow into the main pipe through the liquid phase overflow hole. The hydraulic pressure of the liquid phase above the liquid phase overflow hole due to its static height only provides a secondary driving force. Further... Figure 2-3As shown, to ensure the cover plate 4 can open and close smoothly, the cover plate 4 is provided with a connecting part 41 and a cover plate body 42. The connecting part 41 is fixedly disposed above the second overflow hole 12B on the inner wall of the main pipe. When the cover plate 4 is closed, since the cover plate body 42 is made of ferromagnetic material, it can seal and cover the second overflow hole 12B under magnetic force. The cover plate body 42 and the connecting part 41 are preferably pivotally connected. The pivotal connection can be configured such that the top of the cover plate body 42 rotates around a pin on the connecting part 41 (not shown in the figure). The magnetic force between the annular magnet 3 and the cover plate body 42 can be designed and adjusted according to process conditions. Multiple serrated sections 43 can be evenly provided at the bottom of the cover plate body 42; the design of the serrated sections 43 can disperse the liquid phase.

[0049] Further as Figure 4 , 5 As shown, preferably but not limitingly, the liquid overflow orifice 12 may further include a selectively openable and closable third overflow orifice 12C, the third overflow orifice 12C being positioned higher than the first overflow orifice 12A and the second overflow orifice 12B. To more clearly illustrate the operating state of the third overflow orifice 12C and the corresponding second opening / closing unit, Figure 4 and Figure 5 The first overflow hole 12A and the second overflow hole 12B are not shown in the diagram. The purpose of the selectively openable and closable third overflow hole 12C in this invention is to quickly guide the liquid phase into the main body 1 of the gas-liquid distributor when the liquid level on the gas-liquid distribution plate 2 is too high, thus preventing the liquid from entering the gas phase inlet 11 of the gas-liquid distributor of this invention due to excessive liquid level. Specifically, the opening and closing of the third overflow hole 12C can be controlled by a second opening and closing unit, which includes a sealing plate 6, a connecting rod 7, and a float 8. The float 8 is set at a height lower than the height of the gas phase inlet 11. The upper end of the connecting rod 7 is fixed to the bottom of the float 8, and the lower end is fixed to the sealing plate 6. Under normal operating conditions (i.e., when the liquid level is basically kept low and stable), the sealing plate covers the outside of the third overflow hole 12C. When the liquid level on the outside of the main body 1 exceeds the set height of the float 8, the float 8 drives the sealing plate 6 to move upward through the connecting rod 7 and opens the third overflow hole 12C. To ensure the limiting effect of the float 8, the present invention sets the float on the fixing groove 81 (see reference). Figure 6 Furthermore, the connecting rod 7 is inserted through the perforation on the fixing groove 81. This not only restricts the lateral movement of the float, but also ensures that when the liquid level has not reached the float 8 and the float 8 is in its initial position in the fixing groove 81, the sealing slide plate 6 precisely seals and covers the third overflow hole 12C. Further, as... Figure 6 As shown, the fixing groove 81 is preferably a semi-circular or arc-shaped groove, which can be fixed on the outer wall of the main body 1 of the gas-liquid distributor (at the position below the gas phase inlet). Liquid flow holes 810 can be evenly spaced on the fixing groove 81 to avoid liquid accumulation in the fixing groove.

[0050] Further as Figure 1 , 4 As shown, the flow breaker 5 is fixed to the bottom of the main body 1 by a support member 51. The upper end of the support member 51 is fixedly connected to the lower end of the main body 1, and the lower end of the support member 51 is connected to and supports the flow breaker 5. Further as... Figure 7 As shown, the flow breaker 5 can be made into a solid circular plate, the diameter of which can be equal to or slightly larger than the outer diameter of the main tube 1. The circular plate is provided with toothed portions 50 around its outer edge. The toothed portions 50 can form the gas-liquid mixture from the main tube 1 into a spray state to enhance the gas-liquid mixing and distribution effect. The gas-liquid mixture is evenly sprayed onto the catalyst bed below (not shown in the figure).

[0051] The following is combined Figures 1 to 7 The working principle of the gas-liquid distributor in Embodiment 1 of the present invention will be described in detail below:

[0052] The gas and liquid phases flow from top to bottom (within the hydrogenation reactor). Due to gravity, the liquid phase forms a certain level around the gas-liquid distributor, while the gas phase enters the main pipe 1 through the gas inlet 11 at the top. Because the inner diameter of the main pipe 1 is small, the gas phase can flow at high speed inside the pipe, creating a pressure difference between the inside and outside of the gas-liquid distributor. This pressure difference provides the primary driving force for the liquid phase to flow into the main pipe 1 through the liquid phase overflow hole, while the hydraulic pressure of the liquid phase above the overflow hole due to its static height provides a secondary driving force. Due to the pressure difference, the liquid phase entering through the normally open (i.e., uncovered) first overflow hole 12A is jet-like and forms an atomization effect with the gas phase through perpendicular collision, which enhances gas-liquid mixing.

[0053] When the gas phase load is low (i.e., below the design threshold), the combined effect of the pressure difference and hydraulic force inside and outside the gas-liquid distributor is less than the magnetic force of the annular magnet 3 on the cover plate 4. The cover plate 4 is closed, and the liquid phase cannot pass through the second overflow hole 12B with the cover plate. The flow rate of the liquid phase overflowing into the main pipe 1 is limited (at this time, the liquid phase only enters through the first overflow hole 12A). In the initial closed state of the cover plate 4, the magnetic force between the annular magnet 3 and the cover plate 4 is at its maximum. This magnetic force can resist a certain amount of hydraulic pressure. Under normal operating conditions, when the liquid level has not reached the bottom of the float 8, the sealing slide plate 6, under the combined action of magnetic force, hydraulic force and the pressure difference inside and outside the gas-liquid distributor, effectively prevents the liquid phase from entering the main pipe 1 through the third overflow hole 12C, which is conducive to the accumulation of a higher liquid level on the gas-liquid distribution plate 2. Under the action of two driving forces, the liquid phase enters the main pipe at high speed through the first overflow hole 12A without a cover plate. Since the flow direction of the gas phase and the liquid phase is basically perpendicular, the high-speed gas phase generates shear force on the liquid phase, causing the liquid phase to be cut and broken, thereby achieving a better gas-liquid mixing effect.

[0054] When the gas phase load is large (i.e., higher than the design threshold), the combined effect of the internal and external pressure difference and hydraulic force of the gas-liquid distributor is greater than the magnetic force of the annular magnet 3 on the cover plate 4, and the cover plate 4 opens. At this time, the second overflow hole 12B opens to allow liquid inflow, and the liquid phase flow rate overflowing into the main pipe 1 increases. Under the action of the large internal and external pressure difference, the liquid phase passes through all the first overflow holes 12A and the second overflow hole 12B at a high horizontal velocity. The liquid phase entering the second overflow hole 12B first impacts the cover plate 4 to form an atomization effect. The droplets can flow along the plane of the cover plate body 42 to the serrated part 43 at its lower end. The liquid phase flows into the gaps between the teeth of the serrated part. The high-speed flow of the gas phase is conducive to the atomization and breakup of the liquid phase. The dense liquid flow that converges at the lower part of the main body 1 impacts the baffle plate 5 at high speed. The feed material impacted is splashed and scattered to a larger area outside the central area, thus expanding the liquid phase spraying area of ​​the gas-liquid distributor. In addition, the liquid phase is pulverized and atomized by impacting the baffle plate. Between the teeth of the baffle plate toothed part 50, the liquid phase is further enhanced by the action of the high-speed flowing gas phase, thus enhancing the gas-liquid mixing and distribution effect.

[0055] When the liquid level on the gas-liquid distribution plate 2 becomes too high, the buoyancy of the float 8 causes it to rise, which in turn moves the connecting rod 7 and the connected sealing slide plate 6 upward (the sealing slide plate can be weakly magnetic, generating a certain adsorption force on the outer wall of the main pipe). At this time, the liquid phase enters the main pipe 1 through the third overflow hole 12C, thus effectively preventing the liquid phase from flowing into the gas inlet 11 and affecting the gas-liquid distribution effect. As the liquid level decreases, due to gravity, the float 8 and the connecting rod 7 move downward together until the float 8 is limited to the bottom of the fixed groove 81. At this time, the sealing slide plate 6 returns to its initial position, completely closing the third overflow hole 12C. This invention achieves the above opening and closing effect by reasonably adjusting the size of the float, the surface friction coefficient of the contact surface between the sealing slide plate and the outer wall of the main pipe, and the total mass of the float, connecting rod, and sealing slide plate.

[0056] Example 2

[0057] Embodiment 2 of the present invention provides a hydrogenation reactor (not shown in the figure), which is equipped with the aforementioned gas-liquid distributor. Multiple gas-liquid distributors are evenly distributed and fixedly installed on a gas-liquid distribution plate 2 within the hydrogenation reactor. To further enhance the gas-liquid mixing effect and achieve more uniform spraying, the spacing between the gas-liquid distributors in the hydrogenation reactor is preferably smaller than the diameter of the spray surface formed by the gas-liquid mixture on the catalyst bed.

[0058] 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 gas-liquid distributor, characterized in that, Applications in hydrogenation reactors include: The main body is a vertically arranged tube structure fixed on the gas-liquid distribution plate of the hydrogenation reactor. The gas inlet is located on the top side wall of the main body and is evenly distributed along the circumference of the main body. The gas flows from top to bottom in the main body along the axial direction. A liquid overflow orifice is disposed above the gas-liquid distribution plate and evenly distributed along the circumference of the main pipe. This liquid overflow orifice includes a normally open first overflow orifice and a second overflow orifice that selectively opens and closes due to the pressure difference between the inside and outside of the main pipe. The liquid phase enters the main pipe radially. The selective opening and closing of the second overflow orifice is controlled by a first opening and closing unit, which includes: a ring magnet, fixedly disposed on the outer wall of the main pipe at the corresponding position of the second overflow orifice, the inner diameter of the ring magnet being equal to or greater than the diameter of the second overflow orifice; and a cover plate disposed on the inner wall of the main pipe at the corresponding position of the second overflow orifice. When the gas phase load in the main pipe... When the pressure difference between the inside and outside of the main pipe and the combined hydraulic force are less than the magnetic force exerted by the annular magnet on the cover plate, the cover plate is in a closed state; when the gas phase load inside the main pipe is higher than the threshold, the pressure difference between the inside and outside of the main pipe and the combined hydraulic force are greater than the magnetic force exerted by the annular magnet on the cover plate, the cover plate is in an open state; the cover plate includes: a connecting part, which is fixedly disposed above the second overflow hole on the inner wall of the main pipe; a cover plate body, which seals and covers the second overflow hole and is pivotally connected to the connecting part; a plurality of serrated parts are evenly disposed at the bottom of the cover plate body; the liquid phase overflow hole also includes a selectively openable and closed third overflow hole, the third overflow hole being positioned higher than the first overflow hole and the second overflow hole; A flow-breaking plate, which is disposed at the bottom of the main body, is used to atomize and pulverize the liquid phase; The gas phase flows at high speed in the main pipe with a small inner diameter, creating a pressure difference between the inside and outside of the gas-liquid distributor. This pressure difference provides the main driving force for the liquid phase to flow into the main pipe through the overflow hole. The hydraulic pressure of the liquid phase above the overflow hole due to the static liquid height provides a secondary driving force. Under the action of the two driving forces, the liquid phase enters the main pipe at high speed through the normally open first overflow hole. The high-speed gas phase generates shear force on the liquid phase, causing the liquid phase to be cut and broken. When the cover plate is opened to use the second overflow hole, the liquid phase first impacts the cover plate, which is conducive to the atomization of the liquid phase. A portion of the liquid phase flows along the plane of the cover plate to its lower end. The toothed gaps at the lower end of the cover plate are conducive to the atomization and breaking of the liquid phase.

2. The gas-liquid distributor according to claim 1, characterized in that, The selective opening and closing of the third overflow orifice is controlled by a second opening and closing unit, which includes: The float is positioned at a height lower than the height of the gas inlet. The connecting rod has its upper end fixed to the bottom of the float and its lower end fixed to the sealing plate. The sealing slide plate, under normal operating conditions, seals and covers the outside of the third overflow hole. When the liquid level on the outside of the main body exceeds the set height of the float, the float moves the sealing slide plate upward through the connecting rod and opens the third overflow hole.

3. The gas-liquid distributor according to claim 2, characterized in that, The float is mounted on a fixed groove, and the connecting rod passes through a hole in the fixed groove to limit the float's position.

4. The gas-liquid distributor according to claim 3, characterized in that, The fixing groove is arc-shaped and is fixedly installed on the outer side wall of the main body near the gas phase inlet. Liquid flow holes are evenly arranged on the surface of the fixing groove.

5. The gas-liquid distributor according to claim 1, characterized in that, The flow-breaking plate is fixed to the bottom of the main body by a support member.

6. The gas-liquid distributor according to claim 1, characterized in that, The flow-breaking plate is a solid circular plate with serrated sections around its outer circumference, through which the gas-liquid mixture is sprayed.

7. The gas-liquid distributor according to claim 1, characterized in that, The top of the main body is provided with a top cover, which is a conical panel with the outer edge of the conical panel protruding from the outer side wall of the main body.

8. The gas-liquid distributor according to claim 1, characterized in that, The gas phase inlet is shaped like an inverted triangle.

9. A hydrogenation reactor, characterized in that, Includes a gas-liquid distributor as described in any one of claims 1 to 8, wherein the number of gas-liquid distributors is multiple and they are evenly distributed and fixedly installed on a gas-liquid distribution plate inside the hydrogenation reactor.

10. The hydrogenation reactor according to claim 9, characterized in that, The spacing between the gas-liquid distributors is less than the diameter of the spray surface formed by the gas-liquid mixture on the catalyst bed.

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