Orifice flow disc type liquid distributor suitable for high-viscosity or granular media and use method

Abstract

The invention belongs to the technical field of chemical equipment, and relates to an orifice flow disc type liquid distributor suitable for a high-viscosity or granular medium and a use method. The orifice flow disc type liquid distributor comprises an orifice flow disc, an outer cylinder is arranged on the orifice flow disc, air rising holes and liquid distribution holes are evenly formed in the orifice flow disc, the liquid distribution holes are distributed around the air rising holes, air rising pipes are arranged on the air rising holes, liquid baffles are arranged on the air rising pipes, the liquid distribution holes are of an inverted-cone-shaped structure, rib plates are arranged below the liquid distribution holes, and the rib plates are arranged on the outer cylinder. Liquid distribution plates are arranged at the lower ends of the rib plates. The liquid distribution holes of the inverted-cone-shaped structure are adopted, liquid flowing resistance can be reduced, the diameter of the upper end is large and can rapidly receive liquid in the liquid distribution groove, the diameter of the lower end contracts, local acceleration can be formed, kinetic energy is more stable when the liquid flows out, and uneven liquid outlet caused by flow fluctuation is avoided.

Description

Technical Field

[0001] This invention belongs to the field of chemical equipment technology and relates to a perforated disc liquid distributor suitable for high viscosity or particulate media and its usage method. Background Technology

[0002] In the petrochemical industry, packed towers, as a core mass transfer device, are widely used in various separation and reaction processes due to their simple structure, low pressure drop, and high mass transfer efficiency. Mass transfer, or mass transfer process, typically involves countercurrent or cocurrent contact between gas and liquid on the packing surface to achieve component exchange and separation. The uniformity of gas-liquid distribution is a key factor in ensuring efficient mass transfer. Liquid distributors, as important components in packed towers, can achieve uniform liquid distribution by optimizing the structure between segmented packing layers. This effectively eliminates channeling (the formation of uneven channels in the packing) and wall flow (the flow of liquid along the tower wall), thereby improving the problem of decreased separation efficiency caused by uneven initial distribution and avoiding cross-sectional component imbalance. Liquid distributors are not only a core technological support for improving the overall performance of packed towers but also help solve engineering problems during equipment scale-up. Among various types of liquid distributors, perforated disc liquid distributors are an important category, highly favored in practical applications due to their gas-liquid separation, non-interference, high operational flexibility, and excellent uniformity. Orifice-type liquid distributors are mainly divided into orifice-type and weir-trough type. Theoretically, orifice-type liquid distributors have the best uniform distribution performance and can handle larger flow rates. Therefore, they are widely used in petrochemical, fine chemical and environmental protection fields, and play a key role, especially in large towers.

[0003] Despite their theoretically superior performance, orifice-type liquid distributors still face a series of challenges in practical applications, impacting their efficiency and reliability. For example, the orifices are prone to clogging due to impurities or particulate matter in the material, and corrosion is common in corrosive environments, leading to uneven distribution and operational interruptions. Traditional risers typically have small cross-sectional areas, restricting smooth gas flow and affecting the gas-liquid distribution balance and overall mass transfer efficiency. When processing specific systems, such as high-viscosity liquids or materials containing suspended solids, the orifices on the chassis are more susceptible to clogging, causing localized flow obstruction, channeling, or wall flow phenomena, ultimately reducing separation efficiency and increasing maintenance costs. These problems not only limit the application of orifice-type distributors under harsh conditions but can also lead to performance degradation and operational instability, necessitating in-depth improvements at the structural design level.

[0004] To address the problems encountered in the application of orifice-type liquid distributors, existing technologies have attempted to improve their performance through various means. For example, optimizing the size, shape, and arrangement of the distribution orifices, such as using tapered orifices or increasing the number of orifices, reduces the risk of clogging and improves the uniformity of liquid distribution. Simultaneously, using corrosion-resistant materials such as stainless steel or special alloys to manufacture distributor components extends equipment life. Regarding the issue of small riser cross-sectional area, some designs enhance gas flow capacity by increasing the riser diameter or employing a multi-channel structure, thereby mitigating gas-liquid interference. Furthermore, some improvements introduce self-cleaning mechanisms, such as installing flushing devices inside the distributor or applying surface coating technology to reduce adhesion, helping to address clogging problems caused by specific systems. These methods have improved the operational flexibility and reliability of distributors to some extent and have been applied in practical engineering, especially in applications requiring high flow rates and complex systems.

[0005] However, existing solutions still have significant shortcomings and cannot completely solve the fundamental problems of perforated liquid distributors. For example, while optimizing the distribution hole design can alleviate clogging, clogging still occurs frequently when handling high-viscosity materials or materials containing a large number of solid particles, and the self-cleaning mechanism often increases the complexity and manufacturing cost of the equipment. Improvements to the riser pipe can partially improve gas flow, but increasing the cross-sectional area can lead to a bulky overall distributor structure, affecting installation and maintenance convenience, and may also introduce new flow unevenness problems. Furthermore, while the application of corrosion-resistant materials extends service life, it cannot completely prevent wear and tear in extreme chemical environments and is costly. Overall, existing improvement schemes mostly focus on local optimization and fail to achieve synergistic optimization of gas-liquid distribution from the overall structural perspective. This can lead to efficiency decline and frequent maintenance issues during long-term operation, highlighting the urgent need for more innovative and integrated structural designs. Summary of the Invention

[0006] The purpose of this invention is to provide a perforated disc liquid distributor and its usage method suitable for high-viscosity or particulate media, so as to solve the technical problem that the liquid distribution holes of the bottom plate are easily blocked when the perforated disc liquid distributor is used for a specific system in the prior art.

[0007] To achieve the above objectives, the present invention employs the following technical solution: In a first aspect, this application discloses a perforated flow disk type liquid distributor suitable for high viscosity or particulate media, comprising: a perforated flow disk, an outer cylinder disposed on the perforated flow disk, air rise holes and liquid distribution holes uniformly opened on the perforated flow disk, the liquid distribution holes being distributed around the air rise holes, an air rise pipe disposed on the air rise holes, a baffle plate disposed on the air rise pipe, the liquid distribution holes having an inverted conical structure, and a rib plate disposed below the liquid distribution holes, with a liquid distribution plate disposed at the lower end of the rib plate.

[0008] Preferably, the liquid distribution holes are arranged in a square array, evenly distributed around each air riser 3, and the upper diameter of the inverted conical structure is 2-5 mm larger than the lower diameter or 1.2-2 times the lower diameter.

[0009] Preferably, the cone angle of the inverted cone structure is as follows: When the medium is a low-viscosity, clean liquid, the cone angle should be 30°~60°; When the medium is a high-viscosity liquid containing particles, the cone angle should be 60°~120°.

[0010] Preferably, the height ratio of the outer cylinder to the riser pipe is 1.1 to 1.5:1.

[0011] Preferably, the baffle plate is connected to the air riser pipe through reinforcing ribs. The baffle plate is a round flat plate or an umbrella-shaped baffle plate to block liquid droplets. The diameter of the baffle plate is 1.2 to 2.0 times the diameter of the air riser pipe.

[0012] Preferably, the height of the baffle plate is higher than that of the outer cylinder.

[0013] Preferably, the outer cylinder is welded to the perforated flow plate to form an open cylindrical liquid distribution trough, the outer diameter of which is the difference between the inner diameter of the packed tower and twice the gap, and the gap is the gap between the outer cylinder and the inner wall of the tower.

[0014] Preferably, the riser pipe passes through the perforated flow plate inserted into the riser pipe hole. The riser pipe has a hollow structure with a circular cross-section. The lower end of the riser pipe is flush with the bottom surface of the perforated flow plate and is fixed by welding.

[0015] Preferably, the liquid distribution plate is arc-shaped or flat, and the edge of the liquid distribution plate is fixed to the lower end of the perforated plate by welding with stiffeners.

[0016] Secondly, this application discloses a method of using the orifice flow disk type liquid distributor as described in any one of the above claims, suitable for high-viscosity or particulate media, comprising: The liquid enters the tower from the circulating liquid inlet and flows to the perforated liquid distributor, where it is distributed onto the packing through the liquid distribution plate below the distribution holes. Gas enters the tower from the bottom inlet and flows to the top of the tower through the riser pipe as it passes through the perforated liquid distributor.

[0017] Compared with the prior art, the present invention has the following beneficial effects: The orifice-type liquid distributor disclosed in this application, suitable for high-viscosity or particulate media, adopts an inverted conical structure for the distribution holes, which reduces liquid flow resistance. The larger upper diameter allows for rapid reception of liquid from the distribution channel, while the narrower lower diameter creates local acceleration, resulting in more stable kinetic energy during liquid outflow and preventing uneven liquid distribution caused by flow fluctuations. Secondly, this shape facilitates liquid detachment from the orifice wall, reducing residual material accumulation, and is particularly suitable for high-viscosity or particulate media, reducing the risk of clogging. Furthermore, the inverted conical orifice is easy to machine with a smooth transition at the orifice opening, which weakens the disturbance during liquid outflow, reduces the impact on the packing or tray below, and indirectly improves mass transfer efficiency. At the same time, compared to straight holes, the inclination angle of the orifice wall can guide the liquid to distribute in a predetermined direction, further optimizing the uniformity of liquid distribution. Attached Figure Description

[0018] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of the present invention and should not be regarded as a limitation on the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.

[0019] Figure 1 This is a schematic diagram of the main structure of an embodiment of the present invention; Figure 2 This is a top view of the structure according to an embodiment of the present invention; Figure 3 This is a cross-sectional view of the riser pipe according to an embodiment of the present invention; Figure 4 This is a partial enlarged view of an embodiment of the present invention.

[0020] Wherein: 1-Orifice plate; 2-Outer cylinder; 3-Gas riser pipe; 4-Liquid baffle; 5-Supporting rib; 6-Rib plate; 7-Liquid distribution plate; 8-Liquid distribution hole; 9-Inner wall of tower. Detailed Implementation

[0021] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The components of the embodiments of the present invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0022] Therefore, the following detailed description of the embodiments of the invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of the invention without inventive effort are within the scope of protection of the invention.

[0023] It should be noted that similar labels and letters in the following figures indicate similar items. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0024] In the description of the embodiments of the present invention, it should be noted that if terms such as "upper," "lower," "horizontal," or "inner" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship commonly used when the product of the invention is in use, they are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present invention. Furthermore, terms such as "first" and "second" are only used to distinguish descriptions and should not be construed as indicating or implying relative importance.

[0025] Furthermore, the use of the term "horizontal" does not imply that the component must be absolutely horizontal, but rather that it can be slightly tilted. For example, "horizontal" simply means that its direction is more horizontal than "vertical," and does not mean that the structure must be completely horizontal, but can be slightly tilted.

[0026] In the description of the embodiments of the present invention, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," "connect," and "link" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in the present invention according to the specific circumstances.

[0027] The present invention will now be described in further detail with reference to the accompanying drawings: See Figures 1-4This application discloses a perforated plate type liquid distributor suitable for high-viscosity or particulate media, comprising: a perforated plate 1, an outer cylinder 2 disposed on the perforated plate 1, and uniformly distributed air riser holes and liquid distribution holes 8 on the perforated plate 1, the liquid distribution holes 8 being distributed around the air riser holes, an air riser pipe 3 disposed on the air riser holes, and a baffle plate 4 disposed on the air riser pipe 3. The liquid distribution holes 8 have an inverted conical structure, and the upper diameter of the inverted conical liquid distribution hole must be larger than the lower diameter, the main function of which is to reduce the resistance of liquid flowing into the hole and avoid the formation of local liquid accumulation in the liquid distribution tank. Furthermore, a stiffener 6 is disposed below the liquid distribution hole 8, and a liquid distribution plate 7 is disposed at the lower end of the stiffener 6. This achieves non-interference between gas and liquid, significantly improves the uniformity of gas and liquid distribution on the cross-section of the absorption tower, and at the same time, the large upper diameter allows for rapid liquid reception, while the narrowing lower diameter creates local acceleration, making the liquid outflow kinetic energy more stable, and also facilitates liquid detachment from the hole wall, reducing residue and lowering the risk of blockage in high-viscosity or particulate media.

[0028] In some embodiments, the liquid distribution holes 8 are arranged in a square array, evenly distributed around each air riser 3. The lower diameter of the inverted conical structure is a key parameter that directly affects the liquid discharge effect and needs to be determined according to the designed single-hole flow rate and liquid flow velocity. The upper diameter is 2-5 mm larger than the lower diameter or 1.2-2 times the lower diameter. If the liquid contains particles or has high viscosity, the upper diameter needs to be appropriately increased to facilitate particle passage or reduce adhesion and blockage.

[0029] In some embodiments, the cone angle of the inverted cone structure is specifically: When the medium is a low-viscosity, clean liquid, the cone angle should be 30° to 60°; a smaller cone angle can reduce the diffusion of the liquid during flow and ensure concentrated and stable liquid output.

[0030] When the medium is a high-viscosity liquid containing particles, the cone angle should be between 60° and 120°. A larger cone angle increases the inclination of the channel within the hole, reducing the risk of liquid residue and particle blockage. During the machining of the liquid distribution hole, it is essential to ensure the hole diameter accuracy and that the hole edges are free of burrs.

[0031] In some embodiments, the height ratio of the outer cylinder 2 to the riser pipe 3 is 1.1 to 1.5:1.

[0032] In some embodiments, the baffle plate 4 is connected to the riser pipe 3 via reinforcing ribs 5. The baffle plate 4 is a circular flat plate or an umbrella-shaped plate used to block droplets, and the diameter of the baffle plate 4 is 1.2 to 2.0 times the diameter of the riser pipe 3. If the gas flow rate is high and the droplet size is large, the plate diameter needs to be at the upper limit.

[0033] In some embodiments, the height of the baffle plate 4 is higher than that of the outer cylinder 2.

[0034] In some embodiments, the outer cylinder 2 is welded to the perforated flow plate 1 to form an open cylindrical liquid distribution trough, the outer diameter of which is the difference between the inner diameter of the packed tower and twice the gap, the gap being the gap between the outer cylinder and the inner wall of the tower.

[0035] In some embodiments, the riser pipe 3 is inserted into the riser pipe hole and passes through the perforated flow plate 1. The riser pipe 3 has a hollow structure and a circular cross-section. The lower end of the riser pipe 3 is flush with the bottom surface of the perforated flow plate 1 and is fixed by welding.

[0036] In some embodiments, the liquid distribution plate 7 is arc-shaped or flat, and the edge of the liquid distribution plate 7 is fixed to the lower end of the perforated flow plate by welding with the stiffening plate 6.

[0037] This application also discloses a method for using a perforated disc liquid distributor suitable for high-viscosity or particulate media, characterized by comprising: The liquid enters the tower from the circulating liquid inlet and flows to the perforated liquid distributor. It is then distributed onto the packing through the liquid distribution plate 7 below the distribution hole 9. Gas enters the tower from the bottom inlet and flows to the top of the tower via the riser pipe 3 as it passes through the perforated liquid distributor.

[0038]

Example 1

[0039] The outer cylinder 2 is fixed on the perforated plate 1 to form an open cylindrical groove, i.e., a liquid distribution groove. The diameter of the perforated plate 1 is the same as the outer diameter of the outer cylinder 2, and its thickness needs to be determined comprehensively based on the working conditions, material properties, and structural strength requirements. The gap between the outer cylinder 2 and the inner wall 9 of the tower is controlled within the range of 10~50 mm. The main function of this gap is to serve as an auxiliary channel for gas flow and to balance the gas pressure inside the tower.

[0040] The riser pipes 3 are evenly distributed on the perforated flow plate 1 and serve as the gas phase channel for the packed tower. They are hollow structures with a circular cross-section, allowing gas to rise. The riser pipes 3 are inserted into the perforated flow plate 1, which is evenly distributed across the plate. The riser pipes 3 penetrate the entire perforated flow plate 1 vertically, with their lower ends flush with the bottom surface and fixed by welding. The height of the riser pipes 3 must be higher than that of the liquid distribution holes 8. Their number and dimensions must be determined comprehensively based on the tower diameter, production load, gas flow rate, flow area of ​​a single riser pipe 3, and the available space for the liquid distribution holes 8. The core principle is to ensure that the total flow area of ​​the riser pipes 3 allows for smooth gas passage while maintaining uniform distribution and not encroaching on the effective space of the liquid distribution holes 8.

[0041] The liquid distribution holes 8 are evenly distributed on the perforated flow plate 1, serving as liquid phase channels in the packed tower. They are arranged in a square array, uniformly around each riser pipe 3. The number of liquid distribution holes 8 must be determined based on the uniformity of liquid distribution, taking into account the tower diameter, packing type, liquid flow rate, and the flow capacity of each individual distribution hole 8. This ensures uniform liquid coverage within the tower cross-section, preventing localized flow deviations that could affect mass transfer efficiency. The liquid distribution holes 8 are inverted conical shapes, wider at the top and narrower at the bottom. Below each distribution hole 8 is an arc-shaped or flat liquid distribution plate 7, the edges of which are welded to the lower end of the perforated flow plate 1 using stiffeners 6. The upper diameter of the inverted conical distribution hole 8 must be larger than its lower diameter, primarily to reduce resistance to liquid inflow and prevent localized liquid accumulation within the distribution channel. The lower diameter is a key parameter directly affecting the liquid dispensing effect and needs to be determined based on the designed single-hole flow rate and liquid velocity. Typically, the upper diameter is 2-5 mm larger than the lower diameter, or 1.2-2 times the lower diameter. If the liquid contains particles or has high viscosity, the upper diameter needs to be appropriately increased to facilitate particle passage or reduce adhesion and blockage. Specifically, it depends on the thickness of the liquid distribution plate and the cone angle. For low-viscosity, clean liquids, the cone angle is 30°-60°; a smaller cone angle reduces diffusion during liquid flow, ensuring concentrated and stable dispensing. For high-viscosity, particle-containing liquids, the cone angle is 60°-120°; a larger cone angle increases the inclination of the channel within the hole, reducing the risk of liquid residue and particle blockage. When machining the liquid distribution hole 8, the hole diameter accuracy must be ensured, and the hole edges must be free of burrs.

[0042] The height ratio of the outer cylinder 2 to the riser pipe 3 is controlled within the range of 1.1 to 1.5:1.

[0043] A baffle plate 4 is installed at the upper part of the riser pipe 3, and the riser pipe 3 and the baffle plate 4 are connected by reinforcing ribs. The baffle plate 4 is a round flat plate or umbrella-shaped plate used to block liquid droplets. It needs to be higher than the liquid distribution tank. The diameter of the plate is 1.2 to 2.0 times the diameter of the riser pipe 3. If the gas phase flow rate is high and the droplet size is large, the plate diameter needs to be the upper limit.

[0044]

Example 2

[0045] Example 1: The packed tower has an inner diameter of 800 mm. Liquid enters the tower from the circulating liquid inlet and flows to the distributor, then into the liquid distribution trough formed by welding a perforated flow plate 1 and an outer cylinder 2. From the distribution holes, the liquid flows to the liquid distribution plate and is distributed onto the packing. The thickness of the perforated flow plate 1 and the outer cylinder 2 is 8 mm, the height of the outer cylinder 2 is 250 mm, and the diameter of the perforated flow plate 1 and the outer diameter of the outer cylinder 2 are 760 mm.

[0046] The upper surface of the perforated flow plate 1 is also provided with a riser pipe 3 and liquid distribution holes. One optimal arrangement is to set four liquid distribution holes with an upper diameter of 10 mm, a lower diameter of 5 mm, and a cone angle of 34° at the intersection of the horizontal center line and the vertical center line of the perforated flow plate 1 at 32.5 mm on both sides. Then, these four liquid distribution holes are arranged horizontally or vertically to fill the entire perforated flow plate 1, ensuring that the horizontal and vertical center distance of each liquid distribution hole is 65 mm. In this embodiment, the perforated flow plate 1 can be arranged with a maximum of 96 liquid distribution holes. The arc-shaped liquid distribution plate below each liquid distribution hole is a semi-cylindrical cylinder with a diameter of 6.5 mm, a thickness of 1 mm, and a height of 15 mm.

[0047] To ensure the uniform distribution of liquid distribution holes around the riser pipe 3, a riser pipe hole with a diameter of 50 mm and a riser pipe 3 with an outer diameter of 48.3 mm and a wall thickness of 1 mm are set at the intersection of the centers of every four liquid distribution holes. The riser pipe 3 passes through the riser hole and is connected to the orifice flow plate 1 by welding. The first riser pipe is located at the intersection of the horizontal center line above and the vertical center line 32.5 mm to the left of the horizontal center line of the orifice flow plate 1. Then, the entire orifice flow plate 1 is filled with riser pipe holes according to the above pattern, ensuring that the horizontal and vertical center distance of each riser pipe hole is 130 mm. In this embodiment, the orifice flow plate 1 can be equipped with a maximum of 26 riser pipe holes and riser pipes.

[0048] Gas enters the column through the bottom inlet and flows towards the top of the column via riser pipe 3 after passing through the distributor. Riser pipe 3 is cylindrical. To prevent liquid from overflowing into riser pipe 3, it needs a sufficient height of 170 mm. To further prevent liquid from entering the gas pipe and causing entrainment, and to ensure more stable gas-liquid flow, a baffle plate is added to the riser pipe. The baffle plate is a 70 mm diameter, 2 mm thick disc, positioned 20 mm above the liquid distribution trough. Riser pipe 3 and baffle plate 4 are connected by welding using three evenly distributed reinforcing ribs 5.

[0049] It should be noted that the perforated liquid distributor of the present invention not only achieves the goal of preventing gas and liquid from interfering with each other and significantly improves the uniformity of gas and liquid distribution on the cross section of the absorption tower, but also has a large upper port diameter that can quickly receive liquid, and a narrow lower port diameter that forms local acceleration, making the liquid outflow kinetic energy more stable. It also facilitates the liquid to detach from the orifice wall, reduces residue, and lowers the risk of blockage by high viscosity or particulate media.

[0050] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A orifice flow tray liquid distributor suitable for use with high viscosity or particulate media, characterized in that, include: A perforated plate (1) is provided with an outer cylinder (2). A gas rising hole and a liquid distribution hole (8) are evenly opened on the perforated plate (1). The liquid distribution hole (8) is distributed around the gas rising hole. A gas rising pipe (3) is provided on the gas rising hole. A baffle plate (4) is provided on the gas rising pipe (3). The liquid distribution hole (8) has an inverted conical structure. A rib plate (6) is provided below the liquid distribution hole (8). A liquid distribution plate (7) is provided at the lower end of the rib plate (6).

2. A orifice flow tray liquid distributor suitable for high viscosity or particulate media according to claim 1, wherein, The liquid distribution holes (8) are arranged in a square array and are evenly distributed around each air riser 3. The upper diameter of the inverted conical structure is 2-5 mm larger than the lower diameter or 1.2-2 times the lower diameter.

3. A orifice flow tray liquid distributor suitable for high viscosity or particulate media as claimed in claim 1, wherein, The cone angle of the inverted cone structure is specifically: When the medium is a low-viscosity, clean liquid, the cone angle should be 30°~60°; When the medium is a high-viscosity liquid containing particles, the cone angle should be 60°~120°.

4. A orifice flow tray liquid distributor suitable for high viscosity or particulate media according to claim 1, wherein, The height ratio of the outer cylinder (2) to the riser pipe (3) is 1.1~1.5:

1.

5. A orifice flow tray liquid distributor suitable for high viscosity or particulate media as claimed in claim 1, wherein, The baffle plate (4) is connected to the air riser (3) by a reinforcing rib (5). The baffle plate (4) is a round flat plate or an umbrella-shaped baffle plate to block the liquid droplets. The diameter of the baffle plate (4) is 1.2 to 2.0 times the diameter of the air riser (3).

6. A orifice flow tray liquid distributor suitable for high viscosity or particulate media as claimed in claim 1, wherein, The height of the baffle plate (4) is higher than that of the outer cylinder (2).

7. A orifice flow tray liquid distributor suitable for high viscosity or particulate media as claimed in claim 1, wherein, The outer cylinder (2) is welded to the perforated flow plate (1) to form an open cylindrical liquid distribution trough. The outer diameter is the difference between the inner diameter of the packed tower and twice the gap. The gap is the gap between the outer cylinder and the inner wall of the tower.

8. A orifice flow tray liquid distributor suitable for high viscosity or particulate media as claimed in claim 1, wherein, The riser pipe (3) is inserted into the riser pipe hole and passes through the perforated flow plate (1). The riser pipe (3) is a hollow structure with a circular cross-section. The lower end of the riser pipe (3) is flush with the bottom surface of the perforated flow plate (1) and is fixed by welding.

9. A orifice flow tray liquid distributor suitable for high viscosity or particulate media as claimed in claim 1, wherein, The liquid distribution plate (7) is arc-shaped or flat, and the edge of the liquid distribution plate (7) is fixed to the lower end of the perforated plate by welding with stiffening plates (6).

10. A method of using the orifice flow tray liquid distributor suitable for high viscosity or particulate media as claimed in any one of claims 1 to 9, wherein, include: The liquid enters the tower from the circulating liquid inlet and flows to the perforated liquid distributor. It is then distributed onto the packing through the liquid distribution plate (7) below the distribution hole (9). Gas enters the tower from the bottom inlet and flows to the top of the tower through the riser pipe (3) as it passes through the perforated liquid distributor.

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