CN217940128U - Suction type rotational flow mixing distributor and gas-liquid mixing distribution device - Google Patents

Abstract

The utility model discloses a suction type rotational flow mixing distributor, which mainly comprises a rotational flow mixing cavity, a down pipe and a rotational flow distribution cavity, the whole body is in a vertical dumbbell shape, the rotational flow mixing cavity at the upper part is communicated with the rotational flow distribution cavity at the lower part through the middle down pipe, a spiral mixing channel is arranged in the rotational flow mixing cavity, and a radial distribution channel is arranged in the rotational flow distribution cavity; the suction type rotational flow mixing distributor is fixed on the liquid receiving disc through a down pipe of the suction type rotational flow mixing distributor, the rotational flow mixing cavity is positioned above the liquid receiving disc, and the rotational flow distribution cavity is positioned below the liquid receiving disc; liquid jet holes are uniformly arranged on the wall of the downcomer above the liquid receiving tray. The suction type rotational flow mixing distributor can strengthen the mass transfer process and improve the heat transfer efficiency, and is suitable for being used between catalyst bed layers of a large-diameter downflow reactor. Simultaneously the utility model also discloses a gas-liquid mixture distributor.

Description

Suction type rotational flow mixing distributor and gas-liquid mixing distribution device

Technical Field

The utility model belongs to the petroleum processing field, specifically speaking relates to a suction formula whirl mixing distributor and gas-liquid mixing distribution device.

Background

In the hydrogenation process, because of the exothermic reaction of gas phase, liquid phase and solid phase, in order to make the reaction feed (gas phase and liquid phase) and the catalyst (solid phase) fully, uniformly and effectively contact, a hydrogenation reactor is generally designed with a plurality of catalyst bed layers, a distribution disc is arranged at the top of each bed layer, and a temperature control structure (cold hydrogen box) is arranged between the two bed layers, so as to ensure the safe and stable production of a hydrogenation device and prolong the service life of the catalyst.

The hydrogenation reaction of hydrocarbons belongs to exothermic reaction, for the hydrogenation reactor with multiple beds, the temperature of oil gas and hydrogen will rise after the reaction in the previous bed, and cold hydrogen must be introduced between the two beds to control the temperature for the next bed to continue effective reaction. The tubes that introduce and distribute the cold hydrogen gas inside the reactor are called cold hydrogen tubes. The role and requirements of the cold hydrogen addition system are: uniformly and stably supplying enough cold hydrogen; the cold hydrogen must be thoroughly mixed with the hot reactants and have a uniform temperature and material distribution on entering the next bed. The cold hydrogen pipe is divided into a direct insertion type, a dendritic type and a ring structure according to the form.

The cold hydrogen tank is a combination of a mixing tank and a pre-distribution plate. It is the place where the hot reactant and cold hydrogen in the hydrogenation reactor are mixed and heat exchanged. The reaction product flowing down from the upper layer and the cold hydrogen injected from the cold hydrogen pipe are fully mixed in the box to absorb the reaction heat, reduce the temperature of the reactant, meet the reaction requirement of the next catalyst bed layer and avoid the over-temperature of the reactor.

The first layer of the cold hydrogen box is a baffle plate disk, and the baffle plate is provided with a throttling hole. The cold hydrogen from the cold hydrogen pipe and the oil gas after the reaction of the previous bed layer are premixed on the baffle plate disc and then enter the cold hydrogen box through the throttling hole. Cold hydrogen entering the cold hydrogen box and hot oil gas from the upper layer are repeatedly baffled and mixed, then flow to a second layer of sieve plate disc of the cold hydrogen box, are baffled again on the sieve plate disc to strengthen the mixing effect, and then are distributed. A layer of redistributing tray is arranged below the sieve plate tray for redistributing the oil gas after the predistribution.

The redistributing tray consists of a tray plate and distributors uniformly distributed on the tray plate. The redistribution plate is arranged on the catalyst bed layer, and aims to uniformly distribute the reaction medium, improve the flow condition of the reaction medium, realize good contact with the catalyst and further achieve uniform distribution in the radial direction and the axial direction. The distributors are various, and most of hydrogenation reactors designed and manufactured by China adopt bubble cap type distributors.

Patent CN201610010133.6 provides a rotational flow cold hydrogen pipe of a hydrogenation reactor, which comprises a feeding pipe connected with an outlet of a cold hydrogen storage tank, a distribution ring pipe connected to the feeding pipe, and a plurality of nozzles arranged on the distribution ring pipe, wherein the plurality of nozzles are uniformly distributed around the outer wall of the ring of the distribution ring pipe; the nozzle is cylindrical, the tail end of the side wall of the nozzle is provided with a notch, the tail end of the nozzle is provided with an end cover, and the notches of the nozzles are in the same or opposite directions.

Patent CN201620014039.3 discloses a mixing system comprising: the catalyst comprises a shell, an upper catalyst layer, a lower catalyst layer and a hydrogenation pipe; the upper catalyst layer and the lower catalyst layer are arranged in the shell at intervals from top to bottom, and a mixing cavity is formed between the upper catalyst layer and the lower catalyst layer; one end of the hydrogenation pipe is arranged in the mixing cavity; a plurality of air outlet holes are arranged on the side wall of the hydrogenation pipe. Cold hydrogen flows into the mixing cavity from the plurality of air outlets, the reaction fluid can be fully mixed with the cold hydrogen when flowing into the mixing cavity, and the reaction fluid and the cold hydrogen can be fully mixed when the hydrogenation pipe is introduced with the cold hydrogen, so that the space of the mixing cavity is reduced, but the heat transfer and mass transfer are not uniform enough, and the reaction is not stable enough.

At present, with the upsizing of a hydrogenation device and the development of a new hydrogenation technology, the diameter of a hydrogenation reactor is larger and larger, and the catalyst bed layer of a single hydrogenation reactor is increased. After the hydrogenation reactor is enlarged, the advanced applicability of the inner member becomes more important, and how to realize the uniform distribution of the gas-liquid two-phase fluid in the bed layer, ensure the uniform proceeding of mass transfer and heat transfer and improve the heat transfer efficiency of the medium in the reactor becomes more difficult and more important. For example, the foreign advanced gas-liquid distributor is combined with the advanced catalyst filling technology to ensure that the temperature on the inner section of the reactor is very uniform, and the temperature difference reaches the level of less than or equal to 3 ℃, thereby being beneficial to the operation control of the reactor and greatly prolonging the service life of the catalyst.

SUMMERY OF THE UTILITY MODEL

In order to solve the technical problems that the gas-liquid two-phase fluid in the catalyst bed layer is difficult to distribute uniformly, the mass and heat transfer is not uniform enough and the heat transfer efficiency is low in the prior art, the utility model provides a suction type rotational flow mixing distributor and gas-liquid mixing distribution device.

The utility model provides a suction type rotational flow mixing distributor which mainly comprises a rotational flow mixing cavity, a down pipe and a rotational flow distribution cavity, the whole body is in a vertical dumbbell shape, the rotational flow mixing cavity positioned at the upper part is communicated with the rotational flow distribution cavity positioned at the lower part through the down pipe in the middle; the spiral mixing cavity is composed of a bottom plate, a top plate and a spiral partition plate, the spiral partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the spiral partition plate jointly enclose a spiral mixing channel, an inlet of the spiral mixing channel is positioned on the side surface of the cylinder and forms an inlet of the spiral mixing cavity, an outlet of the spiral mixing channel is positioned in the center of the cylinder and is communicated with a center hole of the bottom plate, the center hole of the bottom plate forms an outlet of the spiral mixing cavity, and the spiral mixing channel gradually reduces in width from outside to inside or keeps the same width; the cyclone distribution cavity consists of a bottom plate, a top plate and a partition plate, the partition plate is in a spiral shape or a straight plate shape, the cyclone distribution cavity is integrally cylindrical, the partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the partition plate jointly enclose a radial distribution channel which is diverged from the center to the periphery, the inlet of the radial distribution channel is positioned at the center of the cylinder and is communicated with the central hole of the top plate, the central hole of the top plate forms the inlet of the cyclone distribution cavity, and the outlet of the radial distribution channel is positioned on the side surface of the cylinder and forms the outlet of the cyclone distribution cavity; the upper end of the downcomer is communicated with a central hole of a bottom plate of the rotational flow mixing chamber, and the lower end of the downcomer is communicated with a central hole of a top plate of the rotational flow distribution chamber; the suction type rotational flow mixing distributor is fixed on the liquid receiving disc through a down pipe of the suction type rotational flow mixing distributor, the rotational flow mixing cavity is positioned above the liquid receiving disc, and the rotational flow distribution cavity is positioned below the liquid receiving disc; liquid spraying holes are uniformly arranged on the pipe wall of the downcomer above the liquid receiving plate.

As an improvement, in order to make the gas-liquid distribution more uniform, the bottom plate of the radial distribution channel is provided with distribution holes.

The liquid jet hole can be provided with a nozzle, so that the collision mixing of cold hydrogen and reaction oil gas can be enhanced, and the temperature of the reaction oil gas can be controlled more effectively.

The utility model also provides a gas-liquid mixing and distributing device, which comprises a reactor shell, and a catalyst grid, a cold hydrogen distributing pipe, a suction type rotational flow mixing distributor, a liquid receiving disc, a gas-liquid distributing pipe and a distributing disc which are arranged in the reactor shell from top to bottom; the cold hydrogen distribution pipe is positioned below the catalyst grating, the liquid receiving disc is fixedly connected with the inner wall of the reactor shell, and the suction type rotational flow mixing distributor is fixed on the liquid receiving disc; the gas-liquid distribution pipe and the distribution plate are positioned below the liquid receiving plate, the distribution plate is fixedly connected with the inner wall of the reactor shell, and the gas-liquid distribution pipe is vertically fixed on the distribution plate.

The gas-liquid distribution pipe adopts short pipes, the outlets at the lower parts of the gas-liquid distribution pipe are in a throat shape with a thin middle part and two large ends, and the aperture ratio (the aperture ratio is defined by the ratio of the total area of the throat section to the radial sectional area of the reactor) of the throat part (the narrowest part of the outlets at the lower parts) is 2-6%; the ratio of the inner diameter of the gas-liquid distribution pipe to the diameter of the throat part is 1.5-3; the aperture ratio of the throat part and the ratio of the inner diameter of the distribution pipe to the diameter of the throat part jointly determine the proper spray angle of the gas-liquid distribution pipe.

As an improvement, a pre-distribution plate is arranged between the liquid receiving plate and the distribution plate, and the pre-distribution plate can make the gas and the liquid distributed more uniformly in the circumferential direction of the reactor shell.

The suction type rotational flow mixing distributor is uniformly distributed in a concentric circle shape by taking the center of the reactor shell as the circle center, and the number of the suction type rotational flow mixing distributor can be determined according to the actual working condition and is generally 2-10.

The utility model provides a gas-liquid mixture distribution device's theory of operation does:

the reaction oil gas of the upper catalyst bed layer flows downwards through the catalyst grating; in order to meet the requirement of the next bed for continuous effective reaction, cold hydrogen is introduced between the two beds to control the temperature, the cold hydrogen is uniformly injected above the liquid receiving disc through a spray hole (or a spray nozzle) of the cold hydrogen distribution pipe, and then enters the cyclone mixing chamber through the inlet of the cyclone mixing chamber and enters the downcomer through the outlet of the cyclone mixing chamber together with most of reaction oil gas; meanwhile, part of liquid phase on the liquid receiving disc enters the descending pipe through the liquid jet holes, enters the rotational flow distribution chamber through the rotational flow distribution chamber inlet together with oil gas entering through the rotational flow mixing chamber inlet, is finally sprayed to the periphery through the rotational flow distribution chamber outlet, and is distributed again through the pre-distribution disc, the gas-liquid distribution pipe and the distribution disc, so that the oil gas is distributed more uniformly on the whole cross section of the reactor, and the reaction of the next bed layer is more stably and effectively carried out.

The utility model discloses following beneficial effect has:

1) The suction type rotational flow mixing distributor can strengthen the mass transfer process, improve the heat transfer efficiency and realize the rapid cooling of high-temperature oil gas;

2) The suction type cyclone mixing distributor mainly comprises a cyclone mixing cavity, a downcomer and a cyclone distribution cavity, has simple and compact structure, saves space, can greatly save the investment of the reactor, is more convenient to install and disassemble, and is suitable for being used between catalyst beds of a large-diameter downflow reactor;

3) The descending pipe section is provided with a liquid jet hole, so that the collision mixing of cold hydrogen and reaction oil gas can be enhanced, and the temperature of the reaction oil gas can be controlled more effectively;

4) The gas-liquid mixing distribution device adopting the suction type rotational flow mixing distributor can be used for large-scale hydrogenation reactors, and the temperature on the inner section of the reactor can be very uniform by combining an advanced catalyst filling technology, so that the operation control of the reactor is facilitated, and the service life of the catalyst can be greatly prolonged;

5) The pre-distribution disc is arranged, so that reaction oil gas is pre-mixed and distributed before being mixed and distributed through the gas-liquid distribution pipe, subsequent mixing and distribution are carried out more thoroughly and uniformly, the reaction is more stable, and the operation of the reactor is easier to control;

6) The specific gas-liquid distribution pipe and the distribution plate are arranged, so that the materials are mixed more uniformly, the operation elasticity is high, and the reaction is more stable.

Drawings

FIG. 1 is a schematic diagram of a suction swirl mixing distributor according to the present invention;

FIG. 2 is a schematic diagram of a spiral mixing channel in a swirl mixing chamber;

FIG. 3 is a schematic view of a radial distribution passage in the swirl distribution chamber;

FIG. 4 is a schematic view of another configuration of radially distributed passages in a swirl distribution chamber;

FIG. 5 is a schematic structural view of the gas-liquid mixing and distributing apparatus of the present invention;

fig. 6 is a schematic view of the structure of the gas-liquid distribution tube of fig. 5.

In the figure: 1-cyclone mixing chamber top plate, 2-cyclone mixing chamber, 3-cyclone mixing chamber spiral clapboard, 4-cyclone mixing chamber bottom plate, 5-cyclone mixing chamber bottom plate center hole, 6-downcomer, 7-cyclone distribution chamber top plate, 8-cyclone distribution chamber clapboard, 9-cyclone distribution chamber bottom plate, 10-cyclone distribution chamber top plate center hole, 11-cyclone distribution chamber, 12-cyclone mixing chamber spiral mixing channel, 13-cyclone distribution chamber radial distribution channel, 14-distribution hole, 15-reactor shell, 16-catalyst grid, 17-catalyst grid supporting beam, 18-cold hydrogen distribution pipe, 19-pipe clamp, 20-suction type cyclone mixing distributor, 21-liquid receiving disc, 22-liquid receiving disc supporting beam, 23-distribution disc, 24-gas-liquid distribution pipe, 25-distribution disc supporting beam, 26-liquid jet hole, 27-pre-distribution disc, 28-lower outlet.

Detailed Description

The present invention will be further described with reference to the accompanying drawings.

As shown in fig. 1, the suction-type cyclone mixing distributor provided by the present invention mainly comprises a cyclone mixing chamber 2, a down pipe 6 and a cyclone distribution chamber 11, and is integrally in the shape of a vertical dumbbell, wherein the cyclone mixing chamber 2 located at the upper part is communicated with the cyclone distribution chamber 11 located at the lower part through the down pipe 6 in the middle; the cyclone mixing cavity 2 is composed of a cyclone mixing cavity bottom plate 4, a cyclone mixing cavity top plate 1 and a cyclone mixing cavity spiral partition plate 3, the whole cyclone mixing cavity 2 is cylindrical, the cyclone mixing cavity spiral partition plate 3 is vertically arranged between the cyclone mixing cavity bottom plate 4 and the cyclone mixing cavity top plate 1, the cyclone mixing cavity bottom plate 4, the cyclone mixing cavity top plate 1 and the cyclone mixing cavity spiral partition plate 3 jointly enclose a cyclone mixing cavity spiral mixing channel 12 (shown in figure 2), an inlet of the cyclone mixing cavity spiral mixing channel 12 is positioned on the side surface of the cylinder, an outlet of the cyclone mixing cavity spiral mixing channel 12 is positioned in the center of the cylinder and is communicated with a cyclone mixing cavity bottom plate center hole 5 (shown in figure 2), and the width of the cyclone mixing cavity spiral mixing channel 12 is gradually reduced from the outside to the inside or keeps the same width; the cyclone distribution cavity 11 consists of a cyclone distribution cavity bottom plate 9, a cyclone distribution cavity top plate 7 and a cyclone distribution cavity partition plate 8, the cyclone distribution cavity partition plate 8 is in a spiral shape (see fig. 3) or a straight plate shape (see fig. 4), the cyclone distribution cavity 11 is wholly cylindrical, the cyclone distribution cavity partition plate 8 is vertically arranged between the cyclone distribution cavity bottom plate 9 and the cyclone distribution cavity top plate 7, the cyclone distribution cavity bottom plate 9, the cyclone distribution cavity top plate 7 and the cyclone distribution cavity partition plate 8 jointly enclose a cyclone distribution cavity radial distribution channel 13 (see fig. 3 and 4) which is diverged from the center to the periphery, an inlet of the cyclone distribution cavity radial distribution channel 13 is positioned at the center of the cylinder and is communicated with a cyclone distribution cavity top plate center hole 10 (see fig. 3 and 4), and an outlet of the cyclone distribution cavity radial distribution channel 13 is positioned on the side surface of the cylinder; the upper end of the down pipe 6 is communicated with a central hole 5 of a bottom plate of the rotational flow mixing cavity, and the lower end of the down pipe 6 is communicated with a central hole 10 of a top plate of the rotational flow distribution cavity; the suction type rotational flow mixing distributor is fixed on a liquid receiving disc 21 through a down pipe 6 of the suction type rotational flow mixing distributor, a rotational flow mixing cavity 2 is positioned above the liquid receiving disc 21, and a rotational flow distribution cavity 11 is positioned below the liquid receiving disc 21; liquid jet holes 26 are uniformly arranged on the pipe wall of the downcomer 6 above the liquid receiving disc 21; the bottom plate of the radial distribution channel 13 of the cyclone distribution cavity is provided with distribution holes 14.

The inlet of the spiral mixing channel 12 of the swirl mixing cavity forms the inlet of the swirl mixing cavity 2, and the central hole 5 of the bottom plate of the swirl mixing cavity forms the inlet of the swirl mixing cavity 2; the central hole 10 of the top plate of the cyclone distribution cavity forms the inlet of the cyclone distribution cavity 11, and the outlet of the radial distribution channel 13 of the cyclone distribution cavity forms the outlet of the cyclone distribution cavity 11.

Wherein, the number of the spiral baffle plates 3 of the rotational flow mixing cavity can be set to be 2-4; the number of the cyclone distribution cavity partition plates 8 can be set to be 4-12.

As shown in fig. 5, the gas-liquid mixing and distributing device of the present invention comprises a reactor shell 15, and a catalyst grid 16, a cold hydrogen distribution pipe 18, a suction type cyclone mixing distributor 20, a liquid receiving plate 21, a gas-liquid distribution pipe 24 and a distribution plate 23, which are arranged in the reactor shell from top to bottom; the cold hydrogen distribution pipe 18 is positioned below the catalyst grid 16 and is fixed on the catalyst grid supporting beam 17 by a pipe clamp 19, the catalyst grid 16 is fixed on the catalyst grid supporting beam 17, the liquid receiving disc 21 is fixed on the distribution disc supporting beam 25 and is fixedly connected with the inner wall of the reactor shell 15, and the suction type rotational flow mixing distributor 20 is fixed on the liquid receiving disc 21; the gas-liquid distribution pipe 24 and the distribution plate 23 are positioned below the liquid receiving plate 21, the distribution plate 23 is fixed on the distribution plate support beam 25 and is fixedly connected with the inner wall of the reactor shell 15, and the gas-liquid distribution pipe 24 is vertically fixed on the distribution plate 23. A predistribution plate 27 is also arranged between the drip pan 21 and the distribution plate 23.

As shown in fig. 6, the lower outlet 28 of the gas-liquid distribution pipe 24 is in the shape of a narrow throat with two large ends, the aperture ratio (the aperture ratio is defined as the ratio of the total area of the throat section to the radial sectional area of the reactor) of the throat (the narrowest part of the lower outlet 28) is 2 to 6%, and the ratio of the inner diameter of the gas-liquid distribution pipe to the diameter of the throat is 1.5 to 3.

The working principle of the present invention is described below with reference to the accompanying drawings 1 to 5:

the oil gas reacted by the upper catalyst bed layer flows downwards through the catalyst grid 16; in order to meet the requirement of the next bed for continuous effective reaction, cold hydrogen is introduced between the two beds to reduce the temperature of reaction oil gas, and the cold hydrogen is injected into the bed space through a cold hydrogen distribution pipe 18, is uniformly distributed in the radial and circumferential directions of the whole section of the reactor and is primarily mixed with the reaction oil gas; after the preliminarily mixed reaction oil gas and cold hydrogen are accumulated on the liquid receiving disc 21, most of the preliminarily mixed reaction oil gas and cold hydrogen enter the cyclone mixing chamber 2 through the spiral mixing channel 12 of the cyclone mixing chamber of the suction type cyclone mixing distributor 20 and enter the downcomer 6 through the central hole 5 of the bottom plate of the cyclone mixing chamber; meanwhile, part of liquid on the liquid receiving disc 21 enters the downcomer 6 through the liquid jet holes 26 on the downcomer 6, then flows through the central hole 10 of the top plate of the cyclone distribution cavity together with oil gas entering the downcomer 6 through the inlet of the cyclone mixing cavity, enters the cyclone distribution cavity 11, flows through the radial distribution channel 13 of the cyclone distribution cavity, and finally flows out through the outlet of the radial distribution channel of the cyclone distribution cavity and the distribution holes 14. The oil gas mixed and distributed by the suction type cyclone mixing distributor 20 is continuously distributed again downwards through the pre-distribution disc 27, the distribution disc 23 and the gas-liquid distribution pipe 24 below, so that the oil gas is distributed more uniformly on the whole cross section of the reactor, and the reaction of the next catalyst bed layer is more effective.

Claims (9)

1. A suction swirl mixing distributor characterized in that: the cyclone mixing chamber positioned at the upper part is communicated with the cyclone distribution chamber positioned at the lower part through the descending pipe in the middle; the spiral mixing cavity is composed of a bottom plate, a top plate and a spiral partition plate, the spiral partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the spiral partition plate jointly enclose a spiral mixing channel, an inlet of the spiral mixing channel is positioned on the side surface of the cylinder and forms an inlet of the spiral mixing cavity, an outlet of the spiral mixing channel is positioned in the center of the cylinder and is communicated with a center hole of the bottom plate, the center hole of the bottom plate forms an outlet of the spiral mixing cavity, and the spiral mixing channel gradually reduces in width from outside to inside or keeps the same width; the cyclone distribution cavity consists of a bottom plate, a top plate and a partition plate, the partition plate is in a spiral shape or a straight plate shape, the cyclone distribution cavity is integrally cylindrical, the partition plate is vertically arranged between the bottom plate and the top plate, the bottom plate, the top plate and the partition plate jointly enclose a radial distribution channel which is diverged from the center to the periphery, the inlet of the radial distribution channel is positioned at the center of the cylinder and is communicated with the central hole of the top plate, the central hole of the top plate forms the inlet of the cyclone distribution cavity, and the outlet of the radial distribution channel is positioned on the side surface of the cylinder and forms the outlet of the cyclone distribution cavity; the upper end of the downcomer is communicated with a central hole of a bottom plate of the rotational flow mixing chamber, and the lower end of the downcomer is communicated with a central hole of a top plate of the rotational flow distribution chamber; the suction type rotational flow mixing distributor is fixed on the liquid receiving disc through a down pipe of the suction type rotational flow mixing distributor, the rotational flow mixing cavity is positioned above the liquid receiving disc, and the rotational flow distribution cavity is positioned below the liquid receiving disc; liquid jet holes are uniformly arranged on the wall of the downcomer above the liquid receiving tray.

2. The aspirating cyclonic mixing distributor of claim 1, wherein: distribution holes are arranged on the bottom plate of the radial distribution channel.

3. The aspirating cyclonic mixing distributor of claim 1, wherein: and a nozzle is arranged on the liquid jet hole.

4. A gas-liquid mixing distribution apparatus using the suction swirl mixing distributor of claim 1, characterized in that: the device comprises a reactor shell, and a catalyst grid, a cold hydrogen distribution pipe, a suction type rotational flow mixing distributor, a liquid receiving disc, a gas-liquid distribution pipe and a distribution disc which are arranged in the reactor shell from top to bottom; the cold hydrogen distribution pipe is positioned below the catalyst grating, the liquid receiving disc is fixedly connected with the inner wall of the reactor shell, and the suction type rotational flow mixing distributor is fixed on the liquid receiving disc; the gas-liquid distribution pipe and the distribution plate are located below the liquid receiving plate, the distribution plate is fixedly connected with the inner wall of the reactor shell, and the gas-liquid distribution pipe is vertically fixed on the distribution plate.

5. The gas-liquid mixture distribution apparatus according to claim 4, characterized in that: and distribution holes are arranged on the bottom plate of the radial distribution channel.

6. The gas-liquid mixture distribution device according to claim 4, characterized in that: and a nozzle is arranged on the liquid jet hole.

7. The gas-liquid mixture distribution device according to claim 4, characterized in that: a pre-distribution disc is arranged between the liquid receiving disc and the distribution disc.

8. The gas-liquid mixture distribution device according to claim 4, characterized in that: the lower outlet of the gas-liquid distribution pipe is in a throat shape with a thin middle part and two large ends, and the aperture ratio of the throat part is 2-6%; the ratio of the inner diameter of the gas-liquid distribution pipe to the diameter of the throat part is 1.5-3.

9. The gas-liquid mixing distribution apparatus according to any one of claims 4 to 8, characterized in that: the suction type rotational flow mixing distributor takes the center of the reactor shell as the circle center and is uniformly distributed with 2-10 concentric circles.

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