Liquid-liquid heterogeneous supergravity reactor device with enhanced macro-micro combination dispersion

Abstract

The invention discloses a macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device, which comprises a liquid distributor I, a liquid distributor II, a macro mixer, a shell and a rotating filler, one end of the liquid distributor I and one end of the liquid distributor II are respectively provided with a liquid feed port I and a liquid feed port II; liquid distribution branch pipes are arranged in the first liquid distributor and the second liquid distributor, the macro mixer is composed of a focusing pipe, a turbulent flow baffle and a mixing pipe, the rotating filler is located in the shell, and the surface of the rotating filler is provided with a sawtooth-shaped protruding structure. And a plurality of convex structures are symmetrically arranged at the same position of the rotating filler in the radial direction. According to the invention, the liquid-liquid two-phase premixing process is enhanced, and uniform macromixing is realized; the liquid-liquid two-phase micro-mixing performance is further improved; the energy utilization rate is high.

Description

Technical Field

[0001] The invention relates to the field of chemical technology and chemical engineering technology, and in particular to a macro-micro combined dispersed and enhanced liquid-liquid heterogeneous supergravity reactor device. Background Art

[0002] Liquid-liquid heterogeneous processes are widely present in the chemical industry, and they are characterized by complex flow characteristics and irregular dispersion processes. In the rapid reaction process between liquid and liquid phases, the reaction is greatly affected by the mixing effect of the reactor. As a typical ultra-gravity intensification equipment, the rotating packed bed can fully break up the liquid-liquid phases, greatly increase the interfacial area, make the two-phase reaction fully proceed, increase the reaction rate and inhibit the occurrence of side reactions.

[0003] In the ultra-gravity reactor, when the liquid-liquid two-phase feed is fed separately, the macroscopic distribution of the liquid depends only on the circumferential rotation of the filler. At the initial position of the filler area, it is difficult to achieve uniform mixing on a macroscopic scale, and more energy (such as increasing the rotation speed) is often required to meet the demand. Therefore, it is very necessary to achieve preliminary macroscopic mixing through premixing before the liquid-liquid two-phase feed contacts the filler. It can achieve initial macroscopic mixing before the liquid-liquid two-phase feed is crushed by the wire mesh. Subsequently, the liquid-liquid two-phase impacts the wire mesh filler in the form of a liquid column jet, which is sheared and crushed by the high-speed rotating wire mesh to form micron-sized liquid microelements, thereby achieving microscopic mixing.

[0004] Liquid-liquid heterogeneous reactions can generally be summarized as the following process (o represents oil phase substances, W represents water phase substances, the following is only a simple summary, and other liquid-liquid heterogeneous processes are applicable to the present invention):

[0005] 2A(o)+B(w)→C(o)+D(w)

[0006] A(o)+B(w)→E

[0007] In this type of reaction process, the rate of the main reaction is generally greater than the rate of the side reaction. In order to promote the full progress of the main reaction, the oil and water phases must be fully mixed. If the mixing is poor, resulting in excessive local concentration of a reactant, a large number of side reactions will occur, greatly reducing the reaction yield and selectivity.

[0008] The following is a specific description of the process of preparing epichlorohydrin by saponification reaction of dichloropropanol and alkali solution, the process of carbon tetraalkylation catalyzed by concentrated sulfuric acid, and the process of preparing vinylidene chloride by saponification reaction of trichloroethane:

[0009] 1. Preparation of epichlorohydrin by saponification reaction of dichloropropanol

[0010] Epichlorohydrin (EPCH), also known as epichlorohydrin, is an important organic chemical raw material and fine chemical intermediate. It is mainly used to produce epoxy resin, nitroglycerin, explosives, fiberglass, plasticizers and other products, and has a broad market. At present, epichlorohydrin is mainly prepared by the reaction of calcium hydroxide and dichloropropanol in industry. The main reaction is as follows:

[0011] 2C3H5Cl2OH+Ca(OH)2→2CH2OCHCH2Cl+CaCl2+H2O(1)

[0012] However, if the oil and water phases cannot fully contact, resulting in excessive local alkali concentration, the excess alkali will easily react with dichloropropanol to produce monochloropropanediol and propylene glycol by the following nucleophilic substitution reaction:

[0013] 2C3H5Cl2OH+Ca(OH)2→2CH2ClCHOHCH2OH+CaCl2(2)

[0014] C3H5Cl2OH+Ca(OH)2→CH2OHCHOHCH2OH+CaCl2(3)

[0015] 2. Concentrated sulfuric acid catalyzed carbon tetraalkylation process

[0016] Alkylate oil prepared from isobutane and butene under strong acid catalysis is the only gasoline blending component that can meet both cleanliness and high octane requirements. At present, the alkylation unit of large-scale refineries mainly adopts the alkylation process with H2SO4 catalyst. The alkylation process involves a series of rapid reactions and the product composition is complex. The main product is TMPs, and the octane number of each component varies greatly. Due to the large difference in polarity between alkanes and H2SO4 and their extremely low mutual solubility, the process is a liquid-liquid two-phase rapid reaction process with complex product distribution. Strengthening the mixing and mass transfer between the acid-hydrocarbon two phases can reduce side reactions and reduce energy consumption, which is of great significance for obtaining high-octane alkylate oil.

[0017] 3. Preparation of vinylidene chloride by saponification reaction of trichloroethane

[0018] Vinylidene chloride monomer is an important polymerization monomer. Its polymer is widely used in fibers, resins, coating adhesives, fireproof materials, food and chemical packaging materials. It is the main monomer for the production of PVDC resin and PVDC latex, and is also an important intermediate for the production of chlorofluorocarbon substitutes. It also plays an important role in the pharmaceutical, dye and other industries. At present, the industry mainly uses trichloroethane and sodium hydroxide saponification reaction to prepare vinylidene chloride, which is a typical liquid-liquid heterogeneous reaction process. The reaction formula is as follows:

[0019] CHCl2CH2Cl+NaOH→CCl2CH2+NaCl+H2O

[0020] CHCl2CH2Cl+NaOH→cis-CHClCHCl+NaCl+H2O

[0021] CHCl2CH2Cl+NaOH→trans-CHClCHCl+NaCl+H2O

[0022] From the above three examples, it can be seen that the requirements for mixing of liquid-liquid heterogeneous phases are extremely high. The ultra-gravity reactor has been widely used in liquid-liquid heterogeneous reaction systems due to its efficient mixing characteristics. However, the feed structure of the existing ultra-gravity reactor is a simple T-shaped premixing tube, so generally, a higher quality product is obtained by increasing the rotation speed and other conditions, which leads to high energy consumption. Through the optimized premixing structure, the liquid-liquid two phases can enter the ultra-gravity reactor in a macro-uniformly mixed state, and further achieve micro-crushing, which will greatly reduce energy consumption and greatly improve reaction efficiency.

[0023] The prior art has the following disadvantages:

[0024] (1) Insufficient premixing of liquid-liquid two-phase reaction process

[0025] At present, the premixing pipeline structure designed for the two feeds of the ultragravity reactor is relatively simple. When the two liquids are miscible, the existing premixing tube can make the two fluids mix evenly on a macroscopic level. However, when the two fluids are not completely miscible (such as the reaction process and extraction process of oil-water two phases), the two-phase fluids generally form a stratified flow pattern with a clear phase interface in the premixing tube, making it difficult to evenly distribute the dispersed phase (a phase with a smaller volume share) in the continuous phase fluid, and the premixing effect achieved is not ideal.

[0026] (II) Conventional rotating packing has limited micro-crushing ability for two-phase liquids

[0027] The current packing mesh is mainly made of smooth metal wire, which works better when dealing with low viscosity systems or low flow rate conditions. However, when the viscosity of the feed liquid is high or the flow rate is fast, the shear effect of the packing decreases, causing the liquid to break up on a larger scale, which in turn leads to poor mass transfer and mixing effects. In particular, as the application of ultra-gravity technology continues to be promoted to the fields of organic matter absorption of gas, oil-water reaction, etc., high viscosity and high flow rate liquid conditions are becoming increasingly frequent.

[0028] In order to solve the above shortcomings, a new type of macro-micro combined dispersed and enhanced liquid-liquid heterogeneous supergravity reactor device is needed. Summary of the invention

[0029] The purpose of the present invention is to solve the shortcomings of the prior art and to propose a macro-micro combined dispersed and enhanced liquid-liquid heterogeneous supergravity reactor device.

[0030] In order to achieve the above object, the present invention adopts the following technical solutions:

[0031] A macro-micro combined dispersion-enhanced liquid-liquid heterogeneous supergravity reactor device, comprising a liquid distributor 1 and a liquid distributor 2, wherein one end of the liquid distributor 1 and the liquid distributor 2 are respectively provided with a liquid feed port 1 and a liquid feed port 2, and the liquid distributor 1 and the liquid distributor 2 are both provided with liquid distribution branches inside;

[0032] A macro mixer, the macro mixer is composed of a focusing tube, a spoiler baffle and a mixing tube;

[0033] The outer shell and the rotating filler are located inside the outer shell, the surface of the rotating filler has a sawtooth convex structure, and the rotating filler is symmetrically provided with two convex structures in the radial direction at the same position.

[0034] As a further technical solution of the present invention, the liquid distributor 1 and the liquid distributor 2 are arranged side by side, and a liquid buffer zone is provided between the liquid feed port 1, the liquid feed port 2 and the liquid distribution branch pipe.

[0035] As a further technical solution of the present invention, the liquid distribution branch pipes are placed in parallel in liquid distributor 1 and liquid distributor 2, and the number of the liquid distribution branch pipes is set according to actual conditions, generally more than 2 groups.

[0036] When the processing volume is large, it is difficult to fully disperse the dispersed phase in the continuous phase through only a single focusing tube. By increasing the number of liquid distribution branches, the liquid passing through each group of liquid distribution branches can be fully macroscopically mixed.

[0037] As a further technical solution of the present invention, the focusing tube is installed at the outlet of the liquid distribution branch pipe, and the other end of the focusing tube is connected to the mixing tube.

[0038] As a further technical solution of the present invention, the spoiler baffles are symmetrically placed in the mixing tube, the inclination angle of the spoiler baffles is 15°-60°, preferably 35°-45°, the spoiler baffles are fixed on the inner wall of the mixing tube, and the number of the spoiler baffles is set according to actual conditions, generally 1-3 groups.

[0039] As a further technical solution of the present invention, the main wall surface of the mixing tube is a wavy structure and is formed of a wear-resistant smooth material, and the inner diameter of the mixing tube remains unchanged.

[0040] The structure achieves disturbance of the two-phase interface by changing the overall flow direction of the two-phase fluid.

[0041] As a further technical solution of the present invention, the rear end of the mixing tube is a variable diameter structure with a smaller inner diameter, the pipe outlet of the mixing tube is aligned with the center position of the rotating filler, and the mixing tube is evenly placed along the circumferential direction in the cavity of the reactor.

[0042] When there are 4 groups of liquid distribution branch pipes, the angle between the pipes is 90°; when there are 6 groups of liquid distribution branch pipes, the angle between the pipes is 60°.

[0043] As a further technical solution of the present invention, the bottom of the reactor is an inclined structure with an inclination angle of 10°-75°, preferably 15°-60°.

[0044] This structure facilitates the downward flow of liquid and avoids liquid retention.

[0045] As a further technical solution of the present invention, a motor is provided under the shell, and a rotating shaft is vertically fixedly installed at the output end of the motor. The rotating shaft extends into the shell and is rotatably connected to the shell, and the top of the rotating shaft is fixedly connected to the bottom of the rotating filler.

[0046] As a further technical solution of the present invention, a sealing assembly is installed at the connection position between the rotating shaft and the shell, and a liquid outlet is opened at one side of the bottom of the shell.

[0047] The beneficial effects of the present invention are:

[0048] 1. The premixing process of the liquid-liquid two-phase is enhanced to achieve uniform macroscopic mixing: the water phase and the oil phase are respectively divided into several streams by the liquid distributor, and each branch is merged by the liquid distribution branch pipe to achieve uniform macroscopic mixing in the liquid distributor; after the liquid-liquid two-phase contact, the phase interface fluctuates. When flowing through the focusing tube, the cross-sectional area of ​​the pipe becomes smaller instantly. Under the condition of constant flow rate, the instantaneous velocity becomes larger, which enhances the radial turbulence effect. In addition, the liquid-liquid two-phase is generally in a stratified form when it first contacts. Under the necking effect of the focusing tube, the radial squeezing effect of the continuous phase on the dispersed phase is enhanced, resulting in a reduction in the size of the dispersed phase liquid layer. It flows through the focusing tube with a smaller size and higher flow rate and enters the mixing tube. Under the action of the spoiler baffle in the tube, the dispersed phase continues to be squeezed continuously, which promotes further fluctuations of the dispersed phase liquid layer, breaks to form smaller daughter fluid microelements, and naturally distributes in the continuous phase liquid layer, so that it is evenly distributed in the continuous phase on a macroscopic scale, increasing the phase interface area and achieving macroscopic mixing.

[0049] 2. The micro-mixing performance of the liquid-liquid two-phase is further improved: a new rotating filler structure is proposed, and its surface has a serrated protrusion structure. When the liquid hits the wire mesh, the protrusion structure on the radial direction of the filler comes into play, causing the liquid jet to tear and break after impact; during the high-speed rotation of the filler, its special circumferential surface structure will produce a high-intensity shear and crushing effect on the liquid-liquid two-phase, and smaller fluid microelements can be obtained, which greatly increases the contact area of ​​the two-phases and improves the reaction rate of the two-phases. Without consuming additional energy, the liquid-liquid two-phases are fully crushed to achieve micro-mixing.

[0050] 3. High energy utilization rate: A liquid distributor and a macro-mixing tube with a new structure are proposed, so that the water-oil two phases are in contact in a number of liquid distribution branches and then mixed by their respective macro-mixing tubes, so that the liquid-liquid two phases can achieve sufficient macro-mixing before contacting the rotating filler; at the same time, the number of liquid mixing branches can be flexibly changed according to different working conditions, so as to achieve sufficient macro-mixing effect without applying additional energy. BRIEF DESCRIPTION OF THE DRAWINGS

[0051] Figure 1 This is a schematic structural diagram of a macro-micro combined dispersion-enhanced liquid-liquid heterogeneous supergravity reactor device proposed by the present invention;

[0052] Figure 2 A schematic diagram of the circumferential distribution of the macroscopic mixing tubes used in the liquid-liquid heterogeneous supergravity reactor device with macro-micro combined dispersion enhancement proposed by the present invention (corresponding to when there are 4 or 6 groups of liquid distribution branches);

[0053] Figure 3 The overall structure and local surface structure of the rotating filler used in the macro-micro combined dispersion-enhanced liquid-liquid heterogeneous supergravity reactor device proposed by the present invention;

[0054] Figure 4 A macro-micro combined dispersed and enhanced liquid-liquid heterogeneous supergravity reactor device proposed by the present invention is used for the process of generating epichlorohydrin by saponification reaction of dichloropropanol, comprising 1-light phase storage tank, 2-heavy phase storage tank, 3-liquid feed pump A, 4-liquid feed pump B, 5-device of the present invention, 6-liquid discharge pump, 7-reactant extraction;

[0055] Figure 5The invention discloses a macro-micro combined dispersed and enhanced liquid-liquid heterogeneous supergravity reactor device for use in a process of generating vinylidene chloride by concentrated sulfuric acid-catalyzed carbon tetraalkylation reaction / trichloroethane saponification reaction, comprising 1-alkane-ene mixed gas tank / oil phase storage tank, 2-acid raw material tank / water phase storage tank, 3-constant temperature tank A, 4-constant temperature tank B, 5-liquid feed pump A, 6-liquid feed pump B, 7-device of the invention, 8-liquid discharge pump, 9-stirring kettle / condensation tank, and 10-reactant extraction.

[0056] Figure 1-2 In: 1. Liquid feed port 1; 2. Liquid feed port 2; 3. Liquid distributor 1; 4. Liquid distributor 2; 5. Liquid distribution branch pipe; 6. Focusing tube; 7. Macro mixing tube; 8. Rotating filler; 9. Shell; 10. Liquid outlet; 11. Sealing assembly; 12. Rotating shaft; 13. Motor. DETAILED DESCRIPTION

[0057] In order to make the technical means, creative features, objectives and effects achieved by the present invention easy to understand, the present invention is further explained below in conjunction with specific implementation methods.

[0058] Please see attached Figure 1 -Attached Figure 3 A macro-micro combined dispersion-enhanced liquid-liquid heterogeneous supergravity reactor device, comprising: a liquid distributor 1 3 and a liquid distributor 2 4, one end of the liquid distributor 1 3 and the liquid distributor 2 4 are respectively provided with a liquid feed port 1 1 and a liquid feed port 2 2, and the liquid distributor 1 3 and the liquid distributor 2 4 are both provided with a liquid distribution branch pipe 5 inside;

[0059] A macro mixer 7, which is composed of a focusing tube 6, a spoiler baffle and a mixing tube;

[0060] The outer shell 9 and the rotating filler 8 are arranged inside the outer shell 9. The surface of the rotating filler 8 has a sawtooth-shaped protrusion structure. The rotating filler 8 has four protrusion structures symmetrically arranged in the radial direction at the same position.

[0061] Please see attached Figure 1 In a preferred embodiment, the liquid distributor 1 3 and the liquid distributor 2 4 are arranged side by side, and a liquid buffer zone is provided between the liquid feed port 1 1 , the liquid feed port 2 2 and the liquid distribution branch pipe 5 .

[0062] Please see attached Figure 1 The liquid distribution branch pipes 5 are placed in parallel in the liquid distributor 1 3 and the liquid distributor 2 4. The number of the liquid distribution branch pipes 5 is set according to actual conditions, generally more than 2 groups.

[0063] When the processing volume is large, it is difficult to fully disperse the dispersed phase in the continuous phase through only a single focusing tube 6. By increasing the number of liquid distribution branches 5, the liquid passing through each group of liquid distribution branches 5 can be fully macroscopically mixed.

[0064] Please see attached Figure 1 The focusing tube 6 is installed at the outlet of the liquid distribution branch pipe 5, and the other end of the focusing tube 6 is connected to the mixing tube.

[0065] Please see attached Figure 1 The spoiler baffles are symmetrically placed in the mixing tube, the inclination angle of the spoiler baffles is 15°-60°, preferably 35°-45°, the spoiler baffles are fixed on the inner wall of the mixing tube, and the number of spoiler baffles is set according to actual conditions, generally 1-3 groups.

[0066] Please see attached Figure 1 The main wall of the mixing tube is a wavy structure and is formed of wear-resistant smooth material, and the inner diameter of the mixing tube remains unchanged.

[0067] The structure achieves disturbance of the two-phase interface by changing the overall flow direction of the two-phase fluid.

[0068] Please see attached Figure 1-2 The rear end of the mixing tube is a variable diameter structure with a smaller inner diameter. The pipe outlet of the mixing tube is aligned with the center position of the rotating filler 8, and the mixing tubes are evenly placed along the circumferential direction in the cavity of the reactor.

[0069] When the liquid distribution branch pipes 5 are in 4 groups, the angle between the pipes is 90°; when the liquid distribution branch pipes 5 are in 6 groups, the angle between the pipes is 60°.

[0070] Please see attached Figure 1 The bottom of the reactor is an inclined structure with an inclination angle of 10°-75°, preferably 15°-60°.

[0071] This structure facilitates the downward flow of liquid and avoids liquid retention.

[0072] Please see attached Figure 1 A motor 13 is provided under the shell 9, and a rotating shaft 12 is vertically fixedly installed at the output end of the motor 13. The rotating shaft 12 extends into the shell 9 and is rotatably connected to the shell 9. The top of the rotating shaft 12 is fixedly connected to the bottom of the rotating filler 8.

[0073] Please see attached Figure 1 A sealing assembly 11 is installed at the connection position between the rotating shaft 12 and the housing 9, and a liquid outlet 10 is opened at one side of the bottom of the housing 9.

[0074] Example 1

[0075] The device and Figure 4The system shown uses dichloropropanol and sodium hydroxide aqueous solution as raw materials to produce epichlorohydrin. The specific steps and results are as follows:

[0076] A sodium hydroxide aqueous solution with a mass fraction of 6% is stored in a light phase storage tank, a chemically pure dichloropropanol liquid is stored in a heavy phase storage tank, the mass flow rate of the sodium hydroxide solution is 1000 g / min, the dichloropropanol liquid is injected into a second feed port at a mass flow rate of 170 g / min, the reaction temperature is controlled at 82° C., the speed of the rotating filling rotor is 1200 r / min, the product discharge time is recorded, and the content of epichlorohydrin therein is sampled and analyzed; after 10 minutes, a stable output product is obtained, and the mass fraction of epichlorohydrin therein is analyzed to be 99.2%.

[0077] With the same process and feed amount, using conventional T-type premixing tube feeding and conventional rotary filler, a stable output product was obtained, and the mass fraction of epichlorohydrin was 92.4%.

[0078] Example 2

[0079] The device and Figure 5 The system shown in the figure carries out the carbon tetraalkylation reaction process catalyzed by concentrated sulfuric acid, and the specific steps and results are as follows:

[0080] H2SO4 is stored in the acid raw material tank, the alkane-olefin ratio in the gas tank is 30:1, the alkane-olefin mixed gas tank is pressurized with nitrogen, the thermostatic bath filled with coolant is started, and the specified temperature is set at 4°C; the flow rates of alkane-olefin and H2SO4 are both 12L / h, the acid-olefin ratio is 1:1, the speed of the rotating filling rotor is 1300r / min, and then the liquid mixture enters the stirring tank through the liquid outlet of the ultra-gravity reactor to continue the reaction, which ends after 15 minutes, and the liquid mixture automatically separates into two phases. The product is stored in the product tank to obtain alkylate oil. After sample analysis, it is found that the product yield is 85% and the octane number is 97.

[0081] With the same reaction process and operating conditions, using conventional T-type premixing tube feeding and conventional rotary filler, the product yield was 74% and the octane number was 93.

[0082] Example 3

[0083] The device and Figure 5 The system is shown in Figure 1. It uses trichloroethane and sodium hydroxide aqueous solution as raw materials to produce vinylidene chloride. The specific steps and results are as follows:

[0084] A sodium hydroxide aqueous solution with a concentration of 0.03 mol / L is stored in a water phase storage tank, and trichloroethane is stored in an oil phase storage tank. The temperature of a thermostatic bath is controlled to rise, and an electronic probe thermometer is used to observe the temperature change in real time. When the temperature rises to 75° C., a circulation pump is turned on to pump trichloroethane into an ultra-gravity reactor to start a reaction. After 10 minutes, the product is condensed and collected to obtain a stable output product, and analysis shows that the yield of the product is 95.4%.

[0085] With the same reaction process and operating conditions, using conventional T-type premixing tube feeding and conventional rotary filler, the product yield was 85%.

[0086] Those skilled in the art should understand that the discussion of any of the above embodiments is merely illustrative and is not intended to imply that the scope of the present invention (including the claims) is limited to these examples. Under the concept of the present invention, the technical features in the above embodiments or different embodiments may be combined, the steps may be implemented in any order, and there are many other variations of the different aspects of the present invention as described above, which are not provided in detail for the sake of simplicity.

[0087] The present invention is intended to cover all such substitutions, modifications and variations that fall within the broad scope of the claims. Therefore, any omissions, modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device, characterized in that: include: A liquid distributor 1 (3) and a liquid distributor 2 (4), wherein one end of each of the liquid distributor 1 (3) and the liquid distributor 2 (4) is provided with a liquid feed port 1 (1) and a liquid feed port 2 (2), respectively, and each of the liquid distributor 1 (3) and the liquid distributor 2 (4) is provided with a liquid distribution branch pipe (5); A macro mixer (7), the macro mixer (7) comprising a focusing tube (6), a spoiler baffle and a mixing tube; A shell (9) and a rotating filler (8), wherein the rotating filler (8) is located inside the shell (9), the surface of the rotating filler (8) has a sawtooth-shaped protrusion structure, and the rotating filler (8) has four protrusion structures symmetrically arranged in the radial direction at the same position.

2. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 1, characterized in that: The liquid distributor 1 (3) and the liquid distributor 2 (4) are arranged side by side, and a liquid buffer zone is provided between the liquid feed port 1 (1), the liquid feed port 2 (2) and the liquid distribution branch pipe (5).

3. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 2, characterized in that: The liquid distribution branch pipes (5) are placed in parallel in the liquid distributor 1 (3) and the liquid distributor 2 (4). The number of the liquid distribution branch pipes (5) is set according to actual conditions, and is generally more than 2 groups.

4. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 3, characterized in that: The focusing tube (6) is installed at the outlet of the liquid distribution branch pipe (5), and the other end of the focusing tube (6) is connected to the mixing tube.

5. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 4, characterized in that: The spoiler baffles are symmetrically placed in the mixing tube, the inclination angle of the spoiler baffles is 15°-60°, preferably 35°-45°, the spoiler baffles are fixed on the inner wall of the mixing tube, and the number of the spoiler baffles is set according to actual conditions, generally 1-3 groups.

6. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 5, characterized in that: The main wall surface of the mixing tube is a wave-shaped structure and is formed of a wear-resistant smooth material, and the inner diameter of the mixing tube remains unchanged.

7. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 6, characterized in that: The rear end of the mixing tube is a variable diameter structure with a smaller inner diameter. The pipeline outlet of the mixing tube is aligned with the center position of the rotating filler (8). The mixing tubes are evenly placed along the circumferential direction in the cavity of the reactor.

8. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 1, characterized in that: The bottom of the reactor is an inclined structure, and the inclination angle is 10°-75°, preferably 15°-60°.

9. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 1, characterized in that: A motor (13) is provided below the housing (9), and a rotating shaft (12) is vertically fixedly installed at the output end of the motor (13). The rotating shaft (12) extends into the interior of the housing (9) and is rotatably connected to the housing (9). The top end of the rotating shaft (12) is fixedly connected to the bottom of the rotating filler (8).

10. The macro-micro combined dispersion-enhanced liquid-liquid heterogeneous high-gravity reactor device according to claim 9, characterized in that: A sealing assembly (11) is installed at the connection position between the rotating shaft (12) and the housing (9), and a liquid outlet (10) is provided on one side of the bottom of the housing (9).

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