Mass transfer enhanced gas-liquid reactor

Abstract

The application discloses a mass transfer enhanced gas-liquid reactor, which is characterized in that a feeding inlet and a tail gas outlet are arranged on a reactor shell, and a discharging outlet is arranged at the bottom; a stirring device comprises at least one group of stirring paddles arranged in the reactor shell; a gas distribution device is fixedly connected in the reactor shell and comprises an outer cover with an upper opening and a lower opening and a gas distributor sleeved in the outer cover, a gas-liquid passage with an annular cross section is formed between the outer cover and the gas distributor, a longitudinal section of the gas-liquid passage is S-shaped, a gas distribution hole is arranged on the side, and a gas inlet pipe is communicated with the gas distribution hole. The mass transfer enhanced gas-liquid reactor has the advantages of promoting the dissolution and transmission of gas, greatly improving the gas atom economy, saving energy, uniform stirring, complete fermentation, fast reaction speed and the like.

Description

Technical Field

[0001] This invention belongs to the field of chemical engineering, specifically relating to a mass transfer enhanced gas-liquid reactor that can be used in industrial reactions involving gas-liquid mass transfer. Background Technology

[0002] Traditional reactors generally include stirred reactors, airlift reactors, membrane reactors, and packed bed reactors. With global technological advancements, gas-liquid reactors have seen new development trends, primarily characterized by the application of high-throughput, miniaturized gas-liquid reactors in process research and optimization, enhancing their gas supply, mixing, and shearing performance. Driven by economic efficiency requirements, processes must meet high-density, high-yield demands; therefore, gas-liquid reactors incorporating novel gas distribution and stirring systems have gained widespread use, improving energy utilization efficiency.

[0003] As a gas-liquid mass transfer reaction process, the volumetric mass transfer coefficient of the gas-liquid system is mainly controlled by the liquid-side mass transfer coefficient and the gas-liquid interphase area 'a'. Comparatively, 'a' has a greater impact on the gas-liquid two-phase mass transfer efficiency and is easier to control. Therefore, increasing 'a' is an effective way to improve the macroscopic reaction rate of gas-liquid. Bubble diameter and gas holdup are two key parameters determining the size of 'a'. Based on the consideration of reducing bubble diameter and improving gas utilization, scientists at home and abroad have attempted to develop ultrafine bubble generation technology to obtain ultrafine bubbles with a diameter of less than 1 mm. They have also developed various new types of reactors, such as stirred self-priming reactors, Venturi reactors, and jet reactors. However, overall, these reactors all have the following shortcomings:

[0004] (1) Insufficient gas-liquid mixing performance: Most reactors only focus on obtaining small-diameter bubbles, while ignoring the gas-liquid ratio, which is a very important parameter in the gas-liquid mass transfer reaction system. Therefore, the ultrafine bubbles they produce can only provide a limited phase interface area and cannot effectively promote the oxidation reaction process.

[0005] (2) Problem of high energy consumption: In order to improve the mixing of local materials with air, a mechanical stirring paddle with high energy consumption will be installed in the reactor to improve the dissolved oxygen mass transfer coefficient. Summary of the Invention

[0006] This invention aims to solve at least one of the technical problems existing in the prior art. To this end, this invention proposes a mass transfer enhanced gas-liquid reactor that can effectively improve gas utilization. This reactor has advantages such as promoting gas dissolution and transfer, significantly improving gas atom economy, saving energy, uniform stirring, thorough reaction, and fast reaction speed.

[0007] To achieve the above objectives, the present invention adopts the following technical solution:

[0008] A mass transfer enhanced gas-liquid reactor includes a reactor shell, a stirring device, an inlet pipe, and a gas distribution device.

[0009] The reactor shell is provided with a feed inlet and a tail gas outlet, and a discharge outlet is provided at the bottom.

[0010] The gas distribution device is fixedly connected inside the reactor shell. The gas distribution device includes an outer cover with upper and lower openings and a gas distributor fitted inside the outer cover. A gas-liquid channel with an annular cross-section is formed between the outer cover and the gas distributor. The longitudinal section of the gas-liquid channel is S-shaped. Gas distribution holes are provided on the side of the gas-liquid channel, and the gas inlet pipe communicates with the gas distribution holes.

[0011] The stirring device includes at least one set of stirring paddles disposed within the reactor shell.

[0012] The stirring device pushes the liquid into the gas-liquid channel of the gas distribution device.

[0013] Both the outer wall of the gas distributor and the inner wall of the outer casing are S-curves forming surfaces of rotation around a virtual central axis, giving the overall shape a vase. The agitator causes the liquid to flow upwards, further leading to the formation of microbubbles. Simultaneously, the microbubbles are carried upwards by the liquid agitated by the agitator, forming an internal circulation backflow in the lower part of the reactor shell through the synergistic effect of the agitator. In addition, the S-shaped gas-liquid channel allows the liquid to flow more closely to the gas distributor, continuously scouring the gas distribution holes, thus causing the bubbles to leave the gas distribution holes before they can grow large, thereby reducing the bubble diameter.

[0014] As a first preferred design of the air distribution device, the air distributor contains a first cavity, the air distribution hole is disposed on the outer surface of the air distributor and communicates with the first cavity, and the air inlet pipe communicates with the first cavity.

[0015] As a second preferred design of the air distribution device, the surface of the air distributor is surrounded by an air distribution pipe, the air inlet pipe is connected to the air distribution pipe, and the air distribution hole is located on the air distribution pipe.

[0016] As a third preferred design of the air distribution device, a second cavity is contained between the inner and outer surfaces of the outer cover, the air distribution hole is disposed on the inner surface of the outer cover and communicates with the second cavity, and the air inlet pipe communicates with the second cavity.

[0017] As a first preferred design of the stirring device, the stirring device further includes a stirring shaft that passes through the bottom of the reactor shell in an airtight manner, and at least one set of the stirring blades is fixedly connected to the stirring shaft below the gas distribution device. In this design, an electric motor is connected to the bottom of the stirring shaft, and the stirring shaft may or may not pass through the gas distribution device.

[0018] As a second preferred design of the stirring device, the stirring device further includes a stirring shaft that passes through the reactor shell airtightly at the top of the reactor shell, with the lower part of the stirring shaft passing through the gas distribution device, and at least one set of stirring blades fixedly connected to the stirring shaft above and below the gas distribution device. In this design, an electric motor is connected to the top of the stirring shaft.

[0019] In this design, preferably, the bottom of the stirring shaft is connected to the bottom of the reactor shell via a bearing. The bearing ensures the stability of the stirring shaft and guarantees the safety of the equipment.

[0020] In this design, preferably, three sets of stirring paddles are equidistantly arranged above the air distribution device. "Equidity" means that adjacent sets of the three stirring paddles are equidistant from each other.

[0021] In this design, preferably, a baffle is also provided inside the reactor shell. The baffle is vertically connected to the inner wall of the reactor shell and has gaps between it and the agitator and the gas distributor. This is to avoid hindering the function of the agitator or the gas distributor. The baffle can help increase turbulence and promote gas-liquid mass transfer.

[0022] In this design, preferably, there are four baffles that are evenly distributed circumferentially within the reactor shell.

[0023] Preferably, the gas-liquid channel has the same width at all heights.

[0024] Preferably, the width of the gas-liquid channel is L, the diameter of the rotating area of ​​the stirring paddle located below the gas distribution device is D1, and L is 0.2 to 0.4 times D1.

[0025] Preferably, the inner diameter of the reactor shell is D, and the diameter of the rotating area of ​​the agitator located below the gas distribution device is D1. When D≥0.25 m, D1 is 0.2~0.25 times D, and when D<0.25 m, D1 is 0.25~0.55 times D.

[0026] Preferably, the diameter of the rotating area of ​​the stirring paddle located above the gas distribution device is D2. When the inner diameter D of the reactor shell is ≥ 0.25 m, D2 is 0.4 to 0.5 times D; when D < 0.25 m, D2 is 0.5 to 0.6 times D.

[0027] Preferably, within the reactor shell, the area above the lowest point of the stirring paddle located above the gas distribution device is the top circulation zone, and the area below it is the bottom circulation zone. The height of the bottom circulation zone is H1, and the height of the top circulation zone is H2. H1 is 0.3 to 0.5 times H2.

[0028] Preferably, the top diameter of the gas distributor is D3, the neck diameter is D4, where D4 is 0.6 to 0.8 times D3; the waist diameter is D5, where D5 is 1.0 to 1.2 times D3; and the bottom diameter is D6, where D6 is 0.7 to 0.9 times D3. The top of the gas distributor is the highest point of the gas-liquid channel; the neck is the height of the point closest to the stirring shaft within the S-shaped gas-liquid channel; the waist is the height of the point furthest from the stirring shaft within the S-shaped gas-liquid channel; and the bottom is the height of the lowest point of the S-shaped gas-liquid channel.

[0029] Preferably, when the inner diameter D of the reactor shell is ≥ 0.25 m, the top diameter D3 of the gas distributor is 0.1 to 0.25 times D; when D < 0.25 m, D3 is 0.25 to 0.55 times D, and the height of the gas distributor is H3, which is 0.7 to 0.9 times D3.

[0030] Preferably, the diameter d of the air distribution hole is 0.1~5 mm, the diameter of the rotating area of ​​the stirring paddle located below the air distribution device is D1, and the distance L1 between adjacent air distribution holes is 0.2~0.5D1.

[0031] Preferably, the air distribution holes at the same height form a ring, and there are a total of 2 to 8 rings of air distribution holes. More preferably, the air distribution holes in each ring are evenly distributed in the height direction.

[0032] Preferably, the angle A between the centerline of the gas-liquid channel and the vertical direction is 0~60°.

[0033] This invention also provides a method of using the above-mentioned mass transfer enhanced gas-liquid reaction, comprising:

[0034] Gas enters the gas distribution device through the inlet pipe, and is dispersed into ultrafine bubbles by the liquid flow in the gas-liquid channel, thus forming an ultrafine bubble flow. This ultrafine bubble flow enters the gas-liquid channel upwards through the gas distribution holes, flowing upwards with the liquid. After overflowing from the top of the outer casing, it moves downwards. Under the action of the stirring paddle located below the gas distribution device, the gas-liquid mixture forms a circulating reflux in the lower inner part of the reactor shell. After the reaction is complete, the product is discharged from the outlet. The generated ultrafine bubbles increase the gas-liquid mass transfer reaction area and improve oxygen utilization.

[0035] Preferably, the gas flow velocity at the air distribution hole is 2~15m / s.

[0036] The beneficial effects of this invention are as follows:

[0037] (1) The mass transfer enhanced gas-liquid reactor provided by the present invention can form micron-sized ultrafine bubbles for gas-liquid reactions, effectively reducing the bubble diameter, increasing the gas-liquid mass transfer area, accelerating the reaction process, and improving oxygen utilization. It is suitable for gas-liquid mass transfer process optimization.

[0038] (2) It has the advantages of saving energy and thorough reaction. The ultrafine bubble flow and the reaction liquid are in full contact in the circulation zone. The bubble flow velocity is greater than 1m / s, which can play a good stirring role and reduce the energy consumption of mechanical stirring. In addition, the reactor shell is equipped with a stirring paddle, which works together with the ultrafine bubble flow to enhance the circulation and reflux effect, thereby saving production costs, reducing energy consumption, improving production efficiency, and creating higher economic benefits. Furthermore, on the one hand, the stirring effect is good, and on the other hand, the dissolved oxygen rate in the liquid is high, which makes the mass transfer more thorough. Attached Figure Description

[0039] The above or additional aspects and advantages of the present invention will become apparent and readily understood from the description of the embodiments taken in conjunction with the following drawings, in which:

[0040] Figure 1 This is a schematic diagram of the mass transfer enhanced gas-liquid reactor in Example 3. Wherein, 2 is the reactor shell, 201 is the exhaust gas outlet, 202 is the air inlet, 203 is the feed inlet, 205 is the gas distributor, 206 is the outer cover, 207 is the fixing rod, 208 is the stirring paddle, 209 is the discharge outlet, 210 is the electric motor, and 211 is the stirring shaft.

[0041] Figure 2 This is a schematic diagram of the air distribution device in Example 1.

[0042] Figure 3 This is a schematic diagram of the air distribution device in Example 2. 116 represents the air distribution pipe.

[0043] Figure 4 This is a schematic diagram of the air distribution device in Embodiment 3. The air distributor is omitted from the drawing, and the dashed lines at the air distribution holes indicate that the holes are located on the inner wall of the outer cover.

[0044] Figure 5 This is a perspective three-dimensional structural diagram of the air distribution device and stirring paddle in Example 2.

[0045] Figure 6 This is a schematic diagram of the mass transfer enhanced gas-liquid reactor in Embodiment 1 of the present invention.

[0046] Wherein, 1 is the reactor shell, 101 is the motor, 102 is the exhaust outlet, 103 is the air inlet, 104 is the stirring shaft, 105 is the feed inlet, 106 is the baffle, 107, 108, and 109 are all stirring paddles, 110 is the gas distributor, 111 is the outer cover, 112 is the fixing rod, 113 is the stirring paddle, 114 is the bearing, and 115 is the discharge port. Detailed Implementation

[0047] Embodiments of the present invention are described in detail below. Examples of these embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain the present invention, and should not be construed as limiting the present invention.

[0048] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "communication" 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 communication between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0049] Example 1

[0050] like Figure 6 , 2 A mass transfer enhanced gas-liquid reactor is shown, comprising a reactor shell 1, a stirring device, an inlet pipe, and a gas distribution device. The reactor shell 1 is provided with an inlet 105 and an outlet 102, and an outlet 115 at the bottom. The stirring device includes a stirring shaft 104 that passes through the reactor shell 1 in an airtight manner at the top of the reactor shell 1, and the stirring shaft 104 is driven by a motor 101. Inside the reactor shell 1, at least one set of stirring paddles is fixedly connected to the stirring shaft 104. Stirring paddles 113 are located below the gas distribution device, and three sets of stirring paddles 107, 108, and 109 are equidistantly fixedly connected to the stirring shaft 104 above the gas distribution device. The lower part of the stirring shaft 104 passes through the gas distribution device. The bottom of the stirring shaft 104 is connected to the bottom of the reactor shell 1 through a bearing 114. The gas distribution device is fixedly connected inside the reactor shell 1. The gas distribution device includes an outer cover 111 with upper and lower openings and a gas distributor 110 sleeved inside the outer cover. A gas-liquid channel with an annular cross-section is formed between the outer cover 111 and the gas distributor 110. The longitudinal section of the gas-liquid channel is S-shaped. A gas distribution hole is provided on the side of the gas-liquid channel. The air inlet pipe is connected to the gas distribution hole.

[0051] The air distributor contains a first cavity, the air distribution hole is disposed on the outer surface of the air distributor and communicates with the first cavity, and the air inlet pipe communicates with the first cavity.

[0052] The gas-liquid channel has the same width at all heights.

[0053] The width of the gas-liquid channel is L, which is 0.2 to 0.4 times D1. D1 is the diameter of the rotating area of ​​the agitator 113.

[0054] The inner diameter of the reactor shell 1 is D, and the diameter of the rotating area of ​​the agitator 113 is D1. When D≥0.25 m, D1 is 0.2~0.25 times D, and when D<0.25 m, D1 is 0.25~0.55 times D.

[0055] The diameter of the rotating area of ​​the stirring paddles 107, 108, and 109 is D2. When the inner diameter D of the reactor shell 1 is ≥ 0.25 m, D2 is 0.4 to 0.5 times D; when D < 0.25 m, D2 is 0.5 to 0.6 times D.

[0056] Inside the reactor shell 1, the height above the lowest point of the stirring paddles 107, 108, and 109 is the top circulation zone, and the height below the lowest point of the stirring paddle 109 is the bottom circulation zone. The height of the bottom circulation zone is H1, and the height of the top circulation zone is H2. H1 is 0.3 to 0.5 times H2.

[0057] The top diameter of the air distributor 110 is D3, the neck diameter of the air distributor 110 is D4, and D4 is 0.6 to 0.8 times D3; the waist diameter of the air distributor 110 is D5, and D5 is 1.0 to 1.2 times D3; the bottom diameter of the air distributor 110 is D6, and D6 is 0.7 to 0.9 times D3.

[0058] When the inner diameter D of the reactor shell 1 is greater than or equal to 0.25 m, the top diameter D3 of the gas distributor 110 is 0.1 to 0.25 times D; when D is less than 0.25 m, D3 is 0.25 to 0.55 times D, and the height of the gas distributor 110 is H3, which is 0.7 to 0.9 times D3.

[0059] The diameter d of the air distribution hole is 0.1~5 mm, and the distance L1 between adjacent air distribution holes is 0.2~0.5D1, where D1 is the diameter of the rotation area of ​​the agitator 113. The function of the agitator 113 is to propel the flow.

[0060] The air distribution holes located at the same height form a ring, and there are a total of two rings of air distribution holes. The air distribution holes in each ring are evenly distributed in the height direction.

[0061] The angle A between the centerline of the gas-liquid channel and the vertical direction is 0~60°.

[0062] The reactor shell 1 is also provided with a baffle 106, which is vertically connected to the inner side wall of the reactor shell 1 and has gaps between it and the stirring paddle and the gas distribution device.

[0063] There are four baffles in total, which are evenly distributed circumferentially inside the reactor shell.

[0064] Using the above-mentioned device, the reactor has a capacity of 5 L, with an inner diameter of 25 cm for the reactor shell, a rotation diameter of 5 cm for the agitator 113, and the following specifications for the gas distributor: top diameter 6.5 cm, neck diameter 4 cm, waist diameter 4.5 cm, bottom diameter 5 cm, and gas distribution hole diameter 1 mm. Compressed gas enters the gas distributor through the inlet pipe. It is then cut and dispersed into ultrafine bubbles by the high-speed liquid flow through the gas-liquid channel, forming an ultrafine bubble flow with a velocity greater than 3 m / s. The bubble flow enters the circulation zone in the lower part of the reactor shell 1 through the micropores, flowing together with the raw material conveyed through the feed inlet 105. Under the synergistic effect of the agitator 113, the formed microbubbles rise upwards inside the outer casing, overflow from the top of the outer casing, and then flow downwards outside the outer casing, forming a gas-liquid mixture. The hydrogenated liquid circulates back within the reactor.

[0065] A chemical plant uses air to oxidize hydrogenated liquid. The original reaction time was 10 minutes. After this method, the oxidation yield is 93% to 96%, and the time required for complete oxidation of the liquid is 7 minutes.

[0066] Example 2

[0067] The only difference between the device used and the device in Embodiment 1 is the air distribution device and the specific size parameters. The air distribution device used in this Embodiment 2 is as follows: the surface of the air distributor is surrounded by an air distribution pipe 116, the air inlet pipe is connected to the air distribution pipe 116, and the air distribution hole is located on the air distribution pipe 116.

[0068] The dimensional parameters are as follows: the inner diameter of the reactor shell 1 is 300cm, the rotation diameter of the agitator 113 is 60cm, and the device specifications of the gas distributor 110 are as follows: the top diameter is 80cm, the neck diameter is 50cm, the waist diameter is 55cm, the bottom diameter is 60cm, and the diameter of the air distribution hole is 3mm.

[0069] An oil refinery uses fresh crude oil to react with hydrogen. After adopting this device, the contact area between hydrogen and liquid phase material increases, which greatly enhances the interphase transfer process. Hydrogen can be fully dissolved in liquid phase material in a supersaturated state, while effectively stripping out impurities such as hydrogen sulfide and ammonia. This significantly improves the hydrogenation reaction performance and increases the desulfurization rate by 25%.

[0070] Example 3

[0071] like Figure 1 , Figure 4 The mass transfer enhanced gas-liquid reactor shown includes a reactor shell 2, a stirring device, an inlet pipe, and a gas distribution device.

[0072] The reactor shell 2 is provided with a feed inlet 203 and a tail gas outlet 201, and a discharge outlet 209 is provided at the bottom.

[0073] The stirring device includes a stirring shaft 211 that passes through the bottom of the reactor shell in an airtight manner, and the stirring shaft 211 is driven by a motor 210; inside the reactor shell 2, the stirring shaft 211 is fixedly connected to a stirring paddle 208, and the stirring paddle 208 is located below the gas distribution device.

[0074] The gas distribution device is fixedly connected inside the reactor shell 2. The gas distribution device includes an outer cover 206 with upper and lower openings and a gas distributor 205 sleeved inside the outer cover 206. A gas-liquid channel with an annular cross-section is formed between the outer cover 206 and the gas distributor 205. The longitudinal section of the gas-liquid channel is S-shaped. A gas distribution hole is provided on the side of the gas-liquid channel. The air inlet pipe is connected to the gas distribution hole.

[0075] The outer cover 206 has a second cavity between its inner and outer surfaces. The air distribution hole is located on the inner surface of the outer cover 206 and communicates with the second cavity. The air inlet pipe communicates with the second cavity.

[0076] The gas-liquid channel has the same width at all heights.

[0077] The width of the gas-liquid channel is L, which is 0.2 to 0.4 times D1. D1 is the diameter of the rotating area of ​​the agitator 208.

[0078] The inner diameter of the reactor shell 2 is D, and the diameter of the rotating area of ​​the agitator 208 is D1. When D≥0.25 m, D1 is 0.2~0.25 times D, and when D<0.25 m, D1 is 0.25~0.55 times D.

[0079] The top diameter of the air distributor is D3, the neck diameter of the air distributor is D4, and D4 is 0.6 to 0.8 times that of D3; the waist diameter of the air distributor is D5, and D5 is 1.0 to 1.2 times that of D3; the bottom diameter of the air distributor is D6, and D6 is 0.7 to 0.9 times that of D3.

[0080] When the inner diameter D of the reactor shell is greater than or equal to 0.25 m, the top diameter D3 of the gas distributor is 0.1 to 0.25 times D; when D is less than 0.25 m, D3 is 0.25 to 0.55 times D, and the height of the gas distributor is H3, which is 0.7 to 0.9 times D3.

[0081] The diameter d of the air distribution hole is 0.1~5 mm, and the distance L1 between adjacent air distribution holes is 0.2~0.5D1.

[0082] The air distribution holes located at the same height form a ring, and there are a total of 2 to 8 rings of air distribution holes. The air distribution holes in each ring are evenly distributed in the height direction.

[0083] The angle A between the centerline of the gas-liquid channel and the vertical direction is 0~60°.

[0084] The reactor used in this device has a capacity of 40 L, with an inner diameter of 50 cm for the reactor shell, a rotation diameter of 12 cm for the agitator 208, and the following specifications for the gas distributor: a top diameter of 10 cm, a neck diameter of 8 cm, a waist diameter of 12 cm, a bottom diameter of 8 cm, and a gas distribution hole diameter of 2 mm. Compressed gas enters the gas distributor through the inlet pipe and is cut and dispersed into ultrafine bubbles by the high-speed liquid flow through the gas-liquid channel. The bubble flow enters the circulation zone at the bottom of the reactor through the micro-pores and flows together with the raw materials conveyed through the feed inlet. Under the synergistic effect of the agitator 208, the formed micro-bubbles rise upward inside the outer cover, overflow from the top of the outer cover, and then flow downward outside the outer cover, forming a gas-liquid mixture. The fermentation liquid forms a circulating reflux within the reactor.

[0085] A small-scale test of this device was conducted at a bio-fermentation plant. As a comparison, the gas distribution device in the device was removed, and cultivation was carried out using the same process. The cultivation results showed that compared with the reactor without the gas distribution device, the cultivation results of the device of the present invention were greatly improved. This was mainly reflected in the fact that after the oxygen mass transfer was enhanced, the reaction time was shortened by 30%, saving resources and energy in the entire production process. At the same time, the good mass transfer effect increased the proportion of viable bacteria in the reactor by about 25%.

[0086] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "illustrative embodiment," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples.

[0087] Although embodiments of the invention have been shown and described, those skilled in the art will understand that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.

Claims

1. A mass transfer enhanced gas-liquid reactor characterized by, The reactor shell, stirring device, gas inlet pipe and gas distribution device, The reactor shell is provided with a feed inlet and a tail gas outlet, and a discharge outlet is arranged at the bottom, The gas distribution device is fixedly connected in the reactor shell, and the gas distribution device comprises an upper and lower open outer cover and a gas distributor sleeved in the outer cover, a gas-liquid passage with an annular cross section is formed between the outer cover and the gas distributor, the longitudinal section of the gas-liquid passage is S-shaped, the side of the gas-liquid passage is provided with a gas distribution hole, and the gas inlet pipe communicates with the gas distribution hole, The stirring device comprises at least one set of stirring paddles arranged in the reactor shell; The at least one set of stirring paddles is below the gas distribution device, and the stirring paddles make the liquid flow upward; The top diameter of the gas distributor is D3, the neck diameter of the gas distributor is D4, D4 is 0.6-0.8 times of D3; the waist diameter of the gas distributor is D5, D5 is 1.0-1.2 times of D3; the bottom diameter of the gas distributor is D6, D6 is 0.7-0.9 times of D3; and the angle A between the center line of the gas-liquid passage and the vertical direction is 0-60°.

2. The mass transfer enhanced gas-liquid reactor according to claim 1, wherein, The gas distribution holes at the same height form a circle, and there are 2-8 circles of gas distribution holes.

3. The mass transfer enhanced gas-liquid reactor according to claim 2, wherein, Each circle of gas distribution holes is uniformly distributed in the height direction.

4. The mass transfer enhanced gas-liquid reactor according to any one of claims 1 to 3, characterized in that The gas distribution device is selected from one of the following three types: The first type: the gas distributor contains a first cavity inside, the gas distribution holes are arranged on the outer surface of the gas distributor and communicate with the first cavity, and the gas inlet pipe communicates with the first cavity; The second type: the gas distributor is surrounded by a gas distribution pipe on the surface, the gas inlet pipe communicates with the gas distribution pipe, and the gas distribution holes are located on the gas distribution pipe; The third type: the outer cover contains a second cavity between the inner and outer surfaces, the gas distribution holes are arranged on the inner surface of the outer cover and communicate with the second cavity, and the gas inlet pipe communicates with the second cavity.

5. The mass transfer enhanced gas-liquid reactor according to claim 1, wherein, The gas-liquid passage is equal in width at each height.

6. The mass transfer enhanced gas-liquid reactor according to claim 5, wherein, The width of the gas-liquid passage is L, the diameter of the rotating area of the stirring paddles below the gas distribution device is D1, and L is 0.2-0.4 times of D1.

7. The mass transfer enhanced gas-liquid reactor according to claim 1, wherein The inner diameter of the reactor shell is D, the diameter of the rotating area of the stirring paddles below the gas distribution device is D1, when D is greater than or equal to 0.25 m, D1 is 0.2-0.25 times of D, and when D is less than 0.25 m, D1 is 0.25-0.55 times of D.

8. The mass transfer enhanced gas-liquid reactor according to claim 1, wherein, The diameter d of the gas distribution hole is 0.1-5 mm, the diameter of the rotating area of the stirring paddles below the gas distribution device is D1, and the distance L1 between adjacent gas distribution holes is 0.2-0.5D1.

9. The mass transfer enhanced gas-liquid reactor according to claim 1, wherein, The stirring device further comprises a stirring shaft that airtightly penetrates the reactor shell at the top of the reactor shell, the lower part of the stirring shaft penetrates the gas distribution device, and at least one set of stirring paddles above and below the gas distribution device are fixedly connected with the stirring shaft.

10. The mass transfer enhanced gas-liquid reactor according to claim 9, wherein, The bottom of the stirring shaft is connected with the bottom of the reactor shell through a bearing.

11. The mass transfer enhanced gas-liquid reactor according to claim 9, wherein, A baffle is further arranged in the reactor shell, and the baffle is vertically connected to the inner side wall of the reactor shell and has a gap between the stirring paddles and the gas distribution device.

12. The mass transfer enhanced gas-liquid reactor according to claim 11, wherein, The baffle plates are four in number and are uniformly distributed in the circumferential direction in the reactor shell.

13. The mass transfer enhanced gas-liquid reactor according to claim 1, wherein, The stirring device further comprises a stirring shaft which airtightly penetrates the reactor shell at the bottom of the reactor shell, and at least one set of the stirring paddles are fixedly connected to the stirring shaft below the gas distribution device.

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