Orifice flow disc type liquid distributor suitable for high gas phase flow velocity and use method

Abstract

The invention belongs to the technical field of chemical equipment, and particularly relates to an orifice flow disc type liquid distributor suitable for high gas phase flow velocity and a use method. The distributor comprises a hole flow disc, an outer cylinder is fixedly connected to the hole flow disc in the circumferential direction, a plurality of gas rising pipes are evenly distributed on the hole flow disc, supporting ribs are arranged on the gas rising pipes, a plurality of layers of liquid baffles are arranged on the supporting ribs, the liquid baffles are all located above the gas rising pipes, and a plurality of liquid distribution holes are formed in the hole flow disc and the periphery of each gas rising pipe. The liquid distribution holes serve as main liquid channels, and gas rises from the gas rising pipe; a plurality of layers of liquid baffles are installed at the top of the riser and strengthen the gas-liquid separation effect through graded interception, so that the problem of liquid foam under the working conditions of high gas speed and high entrainment can be efficiently solved, complex media which are prone to bubbling, high in viscosity and the like are adapted, riser blockage and equipment abrasion are reduced, and the operation stability is improved.

Description

Technical Field

[0001] This invention belongs to the field of chemical equipment technology, specifically relating to a perforated disc liquid distributor suitable for high gas phase flow rates and its usage method. Background Technology

[0002] Packed towers, as core mass transfer equipment in the petrochemical industry, are widely used due to their advantages of simple structure, low pressure drop, and high mass transfer efficiency. Their working principle is based on the counter-current / co-current contact of gas and liquid phases on the packing surface, where the liquid forms a liquid film to transfer mass with the gas, and the flow pattern approximates piston flow. The key to efficient mass transfer lies in the uniformity of gas-liquid distribution, and the liquid distributor is the core component ensuring this condition. Between segmented packing layers, the liquid distributor achieves uniform liquid distribution through optimized structure, effectively eliminating channeling and wall flow phenomena. Studies have shown that a superior liquid distributor can significantly improve the problem of decreased separation efficiency caused by uneven initial distribution, avoid cross-sectional component distribution imbalance, and is a core technological support for improving the overall performance of packed towers and solving scale-up challenges.

[0003] In recent years, perforated disc liquid distributors have been widely used due to their advantages such as large liquid throughput, excellent distribution performance, small footprint within the column, convenient installation, high operational flexibility, and easy leveling. Their main structure consists of a distribution disc with downcomers and a riser assembly, suitable for high-purity separation, multiphase flow, and high liquid load conditions. However, existing perforated disc liquid distributors have certain drawbacks. In conditions with high gas flow velocities and easy liquid foaming, the high-speed rise of the gas phase from the riser can easily impact the liquid surface, leading to severe liquid entrainment, causing liquid loss, gas phase contamination, and riser blockage. It can also cause violent liquid surface fluctuations, disrupting the uniformity of liquid distribution, reducing mass transfer efficiency, and the high-speed entrainment of liquid droplets can exacerbate equipment wear and corrosion. Summary of the Invention

[0004] The purpose of this invention is to provide a perforated plate type liquid distributor and its usage method suitable for high gas phase flow rates, so as to solve the technical problems in the prior art of high gas phase flow rates and easy liquid foaming, which cause liquid loss, gas phase pollution, riser pipe blockage, equipment wear and corrosion caused by high-speed entrainment of liquid droplets.

[0005] To achieve the above objectives, the present invention employs the following technical solution: In the first aspect, this application discloses a perforated flow plate type liquid distributor suitable for high gas phase flow rates, including a perforated flow plate, an outer cylinder fixedly connected to the perforated flow plate in the circumferential direction, a plurality of air risers evenly distributed on the perforated flow plate, a support rib provided on the air riser, a plurality of baffles provided on the support rib, the plurality of baffles being located above the air riser, and a plurality of liquid distribution holes being opened around each air riser on the perforated flow plate.

[0006] Preferably, the outer cylinder is welded to the perforated flow plate to form an open cylindrical trough, i.e., a 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.

[0007] Preferably, the perforated flow plate is provided with a plurality of gas riser holes evenly distributed on it. The gas riser passes through the perforated flow plate by being inserted into the gas riser holes. The gas riser is a gas phase channel of the packed tower. The gas riser has a hollow structure and a circular cross-section. The lower end of the gas riser is flush with the bottom surface of the perforated flow plate and is fixed by welding.

[0008] Preferably, the height ratio of the outer cylinder to the riser pipe is 1.1 to 1.5:1.

[0009] Preferably, the plurality of baffles include a first baffle, a second baffle, and a third baffle; the first baffle, the second baffle, and the third baffle are arranged sequentially from top to bottom above the riser pipe, and the first baffle, the second baffle, and the third baffle are connected by evenly distributed support ribs.

[0010] Preferably, the first baffle is a circular flat plate or an umbrella-shaped baffle to block liquid droplets. The height of the first baffle is higher than that of the outer cylinder, and the diameter of the first baffle is 1.2 to 2.0 times the diameter of the riser pipe.

[0011] Preferably, the second baffle is an open circular plate, through which gas passes, and the opening ratio is 30-50% of the circular plate.

[0012] Preferably, the third baffle plate is a small-hole circular plate, a narrow-slit guide plate, or a microporous grid circular plate, with a smaller opening ratio than the second baffle plate.

[0013] Preferably, the distance between the first baffle, the second baffle and the third baffle is 0.3 to 0.5 times the diameter of the second baffle.

[0014] Secondly, this application discloses a method of using the orifice-disc type liquid distributor suitable for high gas phase flow rates as described in any one of the above claims, comprising: Liquid enters the tower from the circulating liquid inlet and flows to the perforated liquid distributor, where it is distributed from the distribution holes onto the packing. 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. Several layers of baffles further enhance gas-liquid separation by intercepting the liquid in stages.

[0015] Compared with the prior art, the present invention has the following beneficial effects: This application discloses a perforated plate-type liquid distributor suitable for high gas phase flow velocities. The outer cylinder prevents liquid leakage, the riser pipe serves as the gas phase channel, and the distribution holes serve as the liquid phase channel, ensuring uniform liquid distribution. Through an innovative multi-layer baffle design, "staged interception" of the rising airflow is achieved. The outer layer blocks large droplets, the middle layer effectively breaks up and intercepts medium-sized droplets through orifice disturbance, and the inner layer deeply purifies the gas phase. This synergistic effect efficiently solves the problem of droplet entrainment under high gas phase flow velocities and high liquid entrainment conditions, ensuring the cleanliness and efficiency of the gas phase channel. This structure is particularly suitable for complex media such as those prone to foaming and high viscosity. The staged interception mechanism effectively breaks up foam and prevents excessive accumulation of viscous liquid in a single area, thus significantly improving the stability and reliability of the distributor when handling complex conditions. Efficient droplet separation fundamentally reduces the probability of liquid entering the riser pipe, effectively preventing blockage caused by droplet accumulation. Meanwhile, by reducing the direct impact of high-speed droplets on the upper components, corrosion and wear of the equipment are significantly reduced, the overall service life of the equipment is extended, and the long-term, stable and continuous operation of the device is ensured.

[0016] Furthermore, the three-layer baffle plate enhances the gas-liquid separation effect through graded interception. The outer layer blocks large droplets, the middle layer intercepts medium-sized droplets by using orifice disturbance, and the inner layer further purifies the gas phase. It can efficiently solve the droplet problem under high gas velocity and high entrainment conditions, and is suitable for complex media such as easy foaming and high viscosity. It reduces the blockage of the riser pipe and equipment wear, and improves the stability of operation. Attached Figure Description

[0017] 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.

[0018] 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.

[0019] Wherein: 1-Orifice plate; 2-Outer cylinder; 3-Gas riser pipe; 4-First baffle plate; 5-Second baffle plate; 6-Third baffle plate; 7-Supporting rib; 8-Inner wall of the tower; 9-Liquid distribution hole. Detailed Implementation

[0020] 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.

[0021] 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.

[0022] 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.

[0023] 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.

[0024] 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.

[0025] 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.

[0026] The present invention will now be described in further detail with reference to the accompanying drawings: The purpose of this invention is to overcome the shortcomings of the prior art, fundamentally solve the problems of liquid entrainment and uneven liquid distribution, ensure the stable operation and mass transfer efficiency of packed towers, and provide a highly stable perforated plate liquid distributor that is particularly suitable for conditions with high gas flow velocity and easy liquid foaming.

[0027] See Figures 1-3 This application discloses a perforated flow plate type liquid distributor suitable for high gas phase flow rate, including a perforated flow plate 1, an outer cylinder 2 fixedly connected to the perforated flow plate 1 in the circumferential direction, a plurality of air riser pipes 3 evenly distributed on the perforated flow plate 1, a support rib 7 provided on the air riser pipes 3, a plurality of baffle plates provided on the support rib 7, the plurality of baffle plates being located above the air riser pipes 3, and a plurality of liquid distribution holes 9 being opened around each air riser pipe 3 on the perforated flow plate 1.

[0028] In some embodiments, the outer cylinder 2 is welded to the perforated flow plate 1 to form an open cylindrical trough, i.e., a 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.

[0029] In some embodiments, the perforated flow plate 1 is uniformly provided with a plurality of gas riser pipe holes. Gas riser pipes 3 penetrate the perforated flow plate 1 by being inserted into these holes. The gas riser pipes 3 serve as the gas phase channel of the packed tower. The gas riser pipes 3 have a hollow structure and a circular cross-section. The lower end of the gas riser pipe 3 is flush with the bottom surface of the perforated flow plate 1 and is fixed by welding. The gas riser pipes 3 are uniformly distributed on the perforated flow plate 1, serving as the gas phase channel of the packed tower, through which gas rises. The height of the gas riser pipes 3 must be higher than that of the liquid distribution holes 9. The number and size of these pipes must be determined comprehensively based on the tower diameter, production load, gas flow rate, the flow area of ​​a single gas riser pipe 3, and the arrangement space of the liquid distribution holes 9. The core principle is to ensure that the total flow area of ​​the gas riser pipes 3 is sufficient for smooth gas passage, while also ensuring uniform distribution and not encroaching on the effective arrangement space of the liquid distribution holes 9.

[0030] In some embodiments, the height ratio of the outer cylinder 2 to the riser pipe 3 is 1.1 to 1.5:1.

[0031] In some embodiments, the plurality of baffles include a first baffle 4, a second baffle 5, and a third baffle 6; the first baffle 4, the second baffle 5, and the third baffle 6 are arranged sequentially above the riser pipe 3 from top to bottom, and the first baffle 4, the second baffle 5, and the third baffle 6 are connected by evenly distributed support ribs 7.

[0032] In some embodiments, the first baffle plate 4 is a circular flat plate or an umbrella-shaped baffle plate to block liquid droplets. The height of the first baffle plate 4 is higher than that of the outer cylinder 2, and the diameter of the first baffle plate 4 is 1.2 to 2.0 times the diameter of the air riser 3.

[0033] In some embodiments, the second baffle plate 5 is an open circular plate, through which gas passes, and the opening ratio is 30–50% of the circular plate.

[0034] In some embodiments, the third baffle plate 6 is a small-hole circular plate, a narrow-slit guide plate, or a microporous grid circular plate, with an opening ratio less than that of the second baffle plate 5.

[0035] In some embodiments, the distance between the first baffle plate 4, the second baffle plate 5 and the third baffle plate 6 is 0.3 to 0.5 times the diameter of the second baffle plate 5.

[0036] In some embodiments, a perforated liquid distributor suitable for high gas phase flow rates includes: a perforated plate 1, an outer cylinder 2, a riser pipe 3, a first baffle plate 4, a second baffle plate 5, a third baffle plate 6, and supporting ribs 7. The lower end of the outer cylinder 2 is fixed to the perforated plate 1 by welding. The riser pipe 3 and liquid distribution holes 9 are evenly distributed on the perforated plate 1, and the riser pipe 3 is provided with three layers of baffle plates. The outer cylinder 2 is used to prevent liquid leakage, the riser pipe 3 serves as a gas phase channel, and the liquid distribution holes 9 serve as a liquid phase channel to ensure uniform liquid phase distribution.

[0037] The outer cylinder 2 is welded to the perforated flow plate 1 to form an open cylindrical trough, i.e., a liquid distribution trough. Its outer diameter is the difference between the inner diameter of the packed tower and twice the gap (the gap between the outer cylinder 2 and the inner wall 8 of the tower). The thickness needs to be determined comprehensively based on operating conditions, material properties, and structural strength requirements, and can be consistent with the thickness of the perforated flow plate 1. The gap between the outer cylinder 2 and the inner wall of the tower primarily serves as an auxiliary channel for gas flow and to balance the gas pressure inside the tower. It is generally recommended that this gap be controlled within the range of 10~50 mm. The specific gap width needs to be matched with the total cross-sectional area of ​​the riser pipe 3 to ensure that the total gas flow area of ​​both meets the gas flow requirements inside the tower. The height of the outer cylinder 2 needs to be determined comprehensively considering liquid residence time, liquid level stability, overflow prevention, and coordination with the riser pipe 3. The core objective is to ensure that the liquid flows out of the distribution holes 9 uniformly while avoiding gas phase disturbances affecting the liquid level. Typically, the height of the cylinder is designed to be 100~300 mm, and can be determined according to the following principles: the normal liquid level of the uncovered cylindrical tank needs to cover the liquid distribution hole 9; the liquid level should be 50~100 mm higher than the top of the riser pipe 3 to form a liquid seal and prevent liquid from being carried away when the gas phase overflows from the riser pipe 3; considering the fluctuation space, the cylinder height needs to be greater than the liquid level height.

[0038] The riser pipes 3 are evenly distributed on the perforated flow plate 1, serving as the gas phase channel of 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 also evenly distributed. The riser pipes 3 penetrate the entire perforated flow plate 1 vertically, with their lower ends flush with the bottom surface of the plate, and are fixed by welding. The height of the riser pipes 3 must be higher than that of the liquid distribution holes 9. Their number and size must be determined comprehensively based on the tower diameter, production load, gas flow rate, the flow area of ​​a single riser pipe 3, and the available space for the liquid distribution holes 9. 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 for the liquid distribution holes 9.

[0039] 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.

[0040] The upper part of the riser pipe 3 is equipped with three layers of baffles: the riser pipe 3, the first baffle 4, the second baffle 5, and the third baffle 6; these are connected by supporting ribs 7, which are evenly distributed. The outer layer, i.e., the first layer of baffles, is a circular flat plate or an umbrella-shaped baffle to block droplets. It needs to be higher than the liquid distribution trough, and the diameter of the plate is 1.2 to 2.0 times the diameter of the riser pipe 3. If the gas flow velocity is high and the droplet size is large, the plate diameter needs to be at the upper limit. The middle layer, i.e., the second layer, is a perforated circular flat plate, through which gas can pass. The perforation rate is 30-50% of the circular flat plate. The bottom layer, i.e., the first layer, is a circular flat plate with small holes, a narrow slit guide plate, or a microporous mesh circular flat plate. The perforation rate needs to be smaller than that of the second layer of baffles. The spacing between each layer of baffles is 0.3 to 0.5 times the diameter of the baffle.

[0041] This invention discloses a novel perforated flow plate liquid distributor for use in packed towers, relating to the field of chemical equipment technology. The distributor comprises a perforated flow plate 1, an outer cylinder 2, a riser pipe 3, a baffle plate, and supporting ribs 7. The perforated flow plate 1 has a plurality of through holes evenly distributed in a square arrangement. The riser pipe 3 extends vertically through the entire perforated flow plate 1, above the liquid distribution holes 9. The liquid distribution holes 9 serve as the main gas channel, through which gas rises from the riser pipe 3. The riser pipe 3 adopts a hollow structure with a circular cross-section, and multiple riser pipes 3 are evenly distributed on the plate. At the same time, the liquid distribution holes 9 must be evenly distributed around each riser pipe 3. The area between the edge of the liquid distribution groove formed by the orifice flow plate 1 and the outer cylinder 2 and the inner wall of the tower forms a ring-like gas channel, allowing the gas to rise evenly from these channels to the packing layer. Multiple layers of baffles are installed on the top of the riser pipe 3. The three layers of baffles enhance the gas-liquid separation effect through graded interception, which can efficiently solve the liquid droplet problem under high gas velocity and high entrainment conditions. It is suitable for complex media such as easy foaming and high viscosity, reduces the blockage of the riser pipe 3 and equipment wear, and improves the operational stability.

[0042] This application also discloses a method of using a perforated disk type liquid distributor suitable for high gas phase flow rates, including: Liquid enters the tower from the circulating liquid inlet and flows to the perforated liquid distributor, where it is distributed onto the packing from the distribution holes 9. Gas enters the tower from the bottom inlet and flows to the top of the tower through the perforated liquid distributor and riser pipe 3. Several layers of baffles intercept the gas and liquid in stages to enhance gas-liquid separation.

[0043] Example 1: like Figure 1 and Figure 2 As shown in the schematic diagram, the novel perforated liquid distributor of the present invention includes a perforated liquid plate 1, an outer cylinder 2, a riser pipe 3, baffles 4, 5, and 6, and a support rib 7.

[0044] 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, entering the liquid distribution channel formed by welding a perforated plate 1 and an outer cylinder 2. The liquid is then distributed onto the packing through the distribution holes. The thickness of the perforated 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 plate 1 and the outer diameter of the outer cylinder 2 are 760 mm.

[0045] The upper surface of the perforated flow plate 1 is also provided with an air riser pipe 3 and liquid distribution holes. One optimal arrangement is to set four liquid distribution holes with a diameter of 10 mm 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. The perforated flow plate 1 of this embodiment 1 can be arranged with a maximum of 96 liquid distribution holes.

[0046] 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 1, the orifice flow plate 1 can be equipped with a maximum of 26 riser pipe holes and riser pipes.

[0047] Gas enters the tower through the bottom inlet and flows towards the top of the tower via the riser pipe 3, which is cylindrical. To prevent liquid from overflowing into the riser pipe 3, it needs a sufficient height of 150 mm. To further prevent liquid from entering the gas pipe and causing entrainment, and to ensure more stable gas-liquid flow, baffles 4, 5, and 6 are added to the riser pipe. The outer baffle 4 (first layer) is a 5 mm thick, 70 mm diameter disc, positioned above the liquid distribution trough. The middle baffle 5 (second layer) is a 5 mm thick, 60 mm diameter, centrally perforated flat plate with a 40 mm aperture. The bottom baffle 6 (third layer) is a 5 mm thick, 60 mm diameter, centrally perforated flat plate with a 20 mm aperture. The spacing between each baffle layer is 35 mm. The riser pipe 3 and each layer of baffles 4, 5, and 6 are connected by welding using three evenly distributed reinforcing ribs 7.

[0048] 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 efficiently solves the problem of liquid droplets under high gas velocity and high entrainment conditions. It is suitable for complex media such as those that are prone to foaming and have high viscosity, reduces gas riser blockage and equipment wear, and improves operational stability.

[0049] 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 perforated flow plate liquid distributor suitable for high gas phase flow rates, characterized in that, The utility model relates to a kind of liquid distributor, including hole flow disc (1), outer cylinder (2) is fixed along circumference in hole flow disc (1), hole flow disc (1) is evenly distributed with several lift tubes (3), support rib (7) is provided on lift tube (3), several layers of liquid baffle are provided on support rib (7), and several layers of liquid baffle are all located above lift tube (3), every lift tube (3) is evenly distributed with several liquid distribution holes (9) on hole flow disc (1).

2. A hole flow plate liquid distributor suitable for high gas velocity according to claim 1, characterized in that, The outer cylinder (2) and the hole flow disc (1) are welded to form a coverless cylindrical liquid distribution tank, the outer diameter is the difference between the inner diameter of the packing tower and twice the gap, and the gap is the gap between the outer cylinder and the tower inner wall.

3. A hole flow plate liquid distributor suitable for high gas velocity according to claim 1, characterized in that, The hole flow disc (1) is evenly provided with several lift tube holes, the lift tube (3) penetrates the hole flow disc (1) by inserting into the lift tube hole, the lift tube (3) is a gas phase channel of the packing tower, the lift tube (3) has a hollow structure, the cross section is circular, the lower end of the lift tube (3) is flush with the bottom surface of the hole flow disc (1), and is fixed by welding.

4. A hole flow plate liquid distributor suitable for high gas velocity according to claim 1, characterized in that, The height ratio of the outer cylinder (2) to the lift tube (3) is 1.1-1.5:

1.

5. A hole flow plate liquid distributor suitable for high gas velocity according to claim 1, characterized in that, The several layers of liquid baffle include a first liquid baffle (4), a second liquid baffle (5) and a third liquid baffle (6); the first liquid baffle (4), the second liquid baffle (5) and the third liquid baffle (6) are sequentially arranged above the lift tube (3) from top to bottom, and the first liquid baffle (4), the second liquid baffle (5) and the third liquid baffle (6) are connected by evenly distributed support ribs (7).

6. A hole flow plate liquid distributor suitable for high gas velocity according to claim 5, characterized in that, The first liquid baffle (4) is a circular flat plate or an umbrella cap, used to shield liquid drops, and the first liquid baffle (4) is arranged at a height higher than the outer cylinder (2), and the diameter of the first liquid baffle (4) is 1.2-2.0 times the diameter of the lift tube (3).

7. A perforated plate liquid distributor suitable for high gas velocity according to claim 5, wherein, The second liquid baffle (5) is a perforated circular flat plate, and the gas passes through the circular holes, and the opening rate is 30-50% of the circular flat plate.

8. A perforated plate liquid distributor suitable for high gas velocity according to claim 5, wherein, The third liquid baffle (6) is a small-hole circular flat plate, a narrow-slit flow guide plate or a microporous grid circular flat plate, and the opening rate is less than that of the second liquid baffle (5).

9. A perforated plate liquid distributor suitable for high gas velocity according to claim 5, wherein, The spacing between the first liquid baffle (4), the second liquid baffle (5) and the third liquid baffle (6) is 0.3-0.5 times the diameter of the second liquid baffle (5).

10. A method of using a liquid distributor according to any one of claims 1 to 9 for high gas flow rates, characterized in that, The utility model relates to a kind of liquid distributor, including hole flow disc (1), outer cylinder (2) is fixed along circumference in hole flow disc (1), hole flow disc (1) is evenly distributed with several lift tubes (3), support rib (7) is provided on lift tube (3), several layers of liquid baffle are provided on support rib (7), and several layers of liquid baffle are all located above lift tube (3), every lift tube (3) is evenly distributed with several liquid distribution holes (9) on hole flow disc (1). Gas enters the tower from the tower pot gas inlet, flows through the hole flow disc liquid distributor, and flows to the tower top through the lift tube (3), and the several layers of liquid baffles are used for grading interception and strengthening gas-liquid separation. ​

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