A macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device

Abstract

This invention discloses a macro- and micro-combined dispersion-enhanced liquid-liquid heterogeneous hypergravity reactor device, comprising a liquid distributor I and a liquid distributor II, a macro-mixer, a shell, and rotating packing. Liquid distributor I and liquid distributor II are respectively provided with a liquid inlet I and a liquid inlet II at one end. Both liquid distributor I and liquid distributor II have internal liquid distribution branch pipes. The macro-mixer consists of a focusing tube, a baffle plate, and a mixing tube. The rotating packing is located inside the shell, and its surface has a serrated protrusion structure. The rotating packing has symmetrically arranged protrusion structures radially at the same position. This invention enhances the liquid-liquid two-phase premixing process, achieving uniform macro-mixing; further improves the micro-mixing performance of the liquid-liquid two-phase mixture; and achieves high energy utilization.

Description

Technical Field

[0001] This invention relates to the fields of chemical processes and chemical engineering technology, and in particular to a macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device. Background Technology

[0002] Liquid-liquid heterogeneous processes are widely found in the chemical industry, characterized by complex flow characteristics and irregular dispersion processes. In rapid reactions between liquid and liquid phases, the reaction is significantly affected by the mixing effect of the reactor. Rotary packed beds, as a typical example of gravity-enhanced equipment, can thoroughly break up the liquid and liquid phases, greatly increasing the phase interface area, allowing the two-phase reaction to proceed fully, improving the reaction rate, and suppressing the occurrence of side reactions.

[0003] In a high-gravity reactor, when the liquid and liquid phases are fed separately, the macroscopic distribution of the liquid relies solely on the circumferential rotation of the packing material. At the initial position within the packing zone, achieving uniform mixing on a macroscopic scale is difficult, often requiring more energy (e.g., increasing rotational speed) to meet the demand. Therefore, premixing to achieve initial macroscopic mixing before the liquid and liquid phases contact the packing is essential. This allows the liquid and liquid phases to achieve initial macroscopic mixing before being broken up by the wire mesh. Subsequently, the liquid and liquid phases impact the wire mesh packing in the form of liquid jets, where they are sheared and broken up by the high-speed rotating wire mesh, forming micron-sized liquid micro-elements, thus achieving microscopic mixing.

[0004] Liquid-liquid heterogeneous reactions can generally be summarized as follows (o represents oil phase substances, W represents aqueous phase substances; the following is only a simplified summary, and other liquid-liquid heterogeneous processes are also applicable to this invention):

[0005] 2A(o) + B(w) → C(o) + D(w)

[0006] A(o) + B(w) → E

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

[0008] The following examples illustrate the preparation of epichlorohydrin via saponification of dichloropropanol and alkali, the C4 alkylation process catalyzed by concentrated sulfuric acid, and the preparation of vinylidene chloride via saponification of trichloroethane:

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

[0010] Epichlorohydrin (EPCH), also known as epichlorohydrin, is an important organic chemical raw material and fine chemical intermediate. It is mainly used in the production of epoxy resins, nitroglycerin, explosives, fiberglass, plasticizers, and many other products, and has a broad market. Currently, industrially, epichlorohydrin is mainly prepared by reacting calcium hydroxide and dichloropropanol. 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 each other, resulting in excessively high local alkali concentrations, the excess alkali can easily undergo a nucleophilic substitution reaction with dichloropropanol to produce monochloropropanediol and glycerol:

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

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

[0015] 2. Concentrated sulfuric acid-catalyzed C4 alkylation process

[0016] Alkylated oil, prepared from isobutane and butene under strong acid catalysis, is the only gasoline blending component that can simultaneously meet the requirements of cleanliness and high octane number. Currently, large-scale refineries mainly employ alkylation processes using H2SO4 catalysts. The alkylation process involves a series of rapid reactions and produces complex products, primarily TMPs, with significant differences in octane numbers among the various components. Due to the large polarity difference between alkanes and alkenes and their extremely low miscibility with H2SO4, this process is a rapid liquid-liquid two-phase reaction with a complex product distribution. Enhancing the mixing and mass transfer between the acid and hydrocarbon phases can reduce side reactions and energy consumption, which is crucial for obtaining high-octane alkylated oil.

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

[0018] Vinylidene chloride monomer is an important polymerizing monomer with a wide range of applications, including fibers, resins, coatings and adhesives, fire-retardant materials, and food and chemical packaging materials. It is a major monomer in the production of PVDC resins and PVDC latexes, and also an important intermediate in the production of chlorofluorocarbon substitutes. It also plays a significant role in the pharmaceutical and dye industries. Currently, industrially, vinylidene chloride is mainly prepared by the saponification reaction of trichloroethane and sodium hydroxide, a typical liquid-liquid heterogeneous reaction process, as shown in the following reaction formula:

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

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

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

[0022] As the three examples above demonstrate, heterogeneous liquid-liquid reactions require extremely high mixing standards. Due to their efficient mixing characteristics, centrifugal reactors have been widely used in heterogeneous liquid-liquid reaction systems. However, existing centrifugal reactors typically use a simple T-shaped premixing tube for feeding. Therefore, higher quality products are generally obtained by increasing the rotational speed, resulting in high energy consumption. An optimized premixing structure can allow the liquid and liquid phases to enter the centrifugal reactor in a macroscopically homogeneous mixed state, further achieving microscopic fragmentation. This will significantly reduce energy consumption and greatly improve reaction efficiency.

[0023] The existing technology has the following disadvantages:

[0024] (i) Insufficient premixing in the liquid-liquid two-phase reaction process

[0025] Currently, the premixing pipeline structure designed for two feed streams in a supergravity reactor is relatively simple. When the two liquids are miscible, the existing premixing pipe can make the two fluids macroscopically uniformly mixed. However, when the two fluids are not completely miscible (such as in oil-water two-phase reaction processes and extraction processes), the two-phase fluids will generally form a stratified flow pattern with obvious phase interface in the premixing pipe. It is difficult to make the dispersed phase (the phase with a smaller volume proportion) uniformly distributed in the continuous phase fluid, and the premixing effect is not ideal.

[0026] (ii) Conventional rotating packing has limited ability to break up two-phase liquids microscopically.

[0027] Current packing meshes are mainly made of smooth metal wires, which are effective in handling low-viscosity systems or low-flow-rate conditions. However, when the feed liquid has a high viscosity or a high flow rate, the shearing effect of the packing decreases, resulting in larger liquid fragmentation scales, which in turn leads to poorer mass transfer and mixing effects. In particular, with the continuous promotion of the application of hypergravity technology to fields such as organic matter absorbing gas and oil-water reactions, high-viscosity and high-flow-rate liquid conditions are becoming increasingly frequent.

[0028] To address the above shortcomings, a novel macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device is needed. Summary of the Invention

[0029] The purpose of this invention is to address the shortcomings of existing technologies by proposing a macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device.

[0030] To achieve the above objectives, the present invention adopts the following technical solution:

[0031] A macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device includes a liquid distributor one and a liquid distributor two. One end of the liquid distributor one and the liquid distributor two are respectively provided with a liquid inlet one and a liquid inlet two. Both the liquid distributor one and the liquid distributor two are provided with liquid distribution branch pipes inside.

[0032] A macro mixer, comprising a focusing tube, a baffle plate, and a mixing tube;

[0033] The outer shell and the rotating packing are located inside the outer shell. The surface of the rotating packing has a serrated protrusion structure, and the rotating packing has a protrusion structure symmetrically arranged radially at the same position.

[0034] As a further technical solution of the present invention, the liquid distributor one and the liquid distributor two are arranged side by side, and a liquid buffer zone is provided between the liquid inlet one, the liquid inlet two 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 within the liquid distributor one and the liquid distributor two. The number of liquid distribution branch pipes is set according to the actual situation, generally more than two sets.

[0036] When the throughput is large, it is difficult to fully disperse the dispersed phase in the continuous phase using only a single focusing tube. By increasing the number of liquid distribution branches, the liquid passing through each set 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 turbulence baffles are symmetrically placed inside the mixing tube, the inclination angle of the turbulence baffles is 15°-60°, preferably 35°-45°, the turbulence baffles are fixed on the inner wall of the mixing tube, and the number of turbulence baffles is set according to the actual situation, generally 1-3 sets.

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

[0040] This 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 outlet of the mixing tube is aligned with the center position of the rotating packing, and the mixing tube is uniformly placed circumferentially in the cavity of the reactor.

[0042] When there are 4 groups of liquid distribution branches, the included angle between the branches is 90°; when there are 6 groups of liquid distribution branches, the included angle between the branches 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 prevents liquid stagnation.

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

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

[0047] The beneficial effects of this invention are as follows:

[0048] 1. The liquid-liquid two-phase premixing process is enhanced, achieving uniform macroscopic mixing: The aqueous and oil phases are divided into several streams by the liquid distributor, and the streams converge through the liquid distribution branch pipes, achieving uniform macroscopic mixing within the liquid distributor. After the liquid-liquid two phases come into contact, phase interface fluctuations occur. When flowing through the focusing pipe, the cross-sectional area of ​​the pipe decreases instantaneously, and the instantaneous velocity increases under constant flow conditions, enhancing radial turbulence. In addition, the liquid-liquid two phases are generally in a stratified state when they first come into contact. Under the constriction effect of the focusing pipe, the radial compression of the dispersed phase by the continuous phase is enhanced, resulting in a reduction in the size of the dispersed phase liquid layer. It flows through the focusing pipe with a smaller size and higher flow velocity, entering the mixing pipe. Under the action of the turbulence baffles inside the pipe, the dispersed phase continues to be subjected to continuous compression, promoting further fluctuations in the dispersed phase liquid layer, breaking into smaller daughter fluid micro-elements, which are naturally distributed in the continuous phase liquid layer, making them uniformly distributed in the continuous phase macroscopically, increasing the phase interface area, and achieving macroscopic mixing.

[0049] 2. The micro-mixing performance of liquid-liquid two-phase systems is further improved: A novel rotating packing structure is proposed, which has a serrated protrusion structure on its surface. When the liquid impacts the wire mesh, the radial protrusion structure of the packing plays a role, causing the liquid jet to tear and break after impact. During the high-speed rotation of the packing, its special circumferential surface structure will produce a high-intensity shearing and breaking effect on the liquid-liquid two-phase system, which can obtain smaller fluid micro-elements, greatly increasing the contact area between the two phases and improving the reaction rate of the two phases. Without consuming additional energy, the liquid-liquid two-phase system is fully broken up, achieving micro-mixing.

[0050] 3. High energy utilization: A liquid distributor and a macro-mixing pipe with a novel structure are proposed, which allows the water and oil phases to come into contact in several liquid distribution branches and then be mixed by their respective macro-mixing pipes, so that the liquid and liquid phases can achieve sufficient macro-mixing before contacting the rotating packing. 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. Attached Figure Description

[0051] Figure 1 This is a schematic diagram of the structure of a macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device proposed in this invention.

[0052] Figure 2 This is a schematic diagram of the circumferential distribution of the macroscopic mixing pipes used in the macroscopic-microscopic combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device proposed in this invention (when there are 4 or 6 sets of liquid distribution branch pipes).

[0053] Figure 3 This invention relates to the overall structure and local surface structure of the rotating packing material used in a macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device.

[0054] Figure 4 The present invention proposes a macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device for the saponification reaction of dichloropropanol to produce epichlorohydrin, comprising 1-light phase storage tank, 2-heavy phase storage tank, 3-liquid feed pump A, 4-liquid feed pump B, 5-the device of the present invention, 6-liquid discharge pump, and 7-reactant collection.

[0055] Figure 5The present invention proposes a macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device for the process of concentrated sulfuric acid catalytic C4 alkylation reaction / trichloroethane saponification reaction to produce vinylidene chloride, comprising: 1-an alkene mixed gas tank / oil phase storage tank, 2-acid feed tank / aqueous phase storage tank, 3-thermostatic bath A, 4-thermostatic bath B, 5-liquid feed pump A, 6-liquid feed pump B, 7-the device of the present invention, 8-liquid discharge pump, 9-stirred vessel / condenser, and 10-reactant collection.

[0056] Figure 1-2 In the middle section: 1. Liquid inlet one; 2. Liquid inlet two; 3. Liquid distributor one; 4. Liquid distributor two; 5. Liquid distribution branch pipe; 6. Focusing pipe; 7. Macro mixing pipe; 8. Rotating packing; 9. Outer shell; 10. Liquid outlet; 11. Sealing assembly; 12. Rotating shaft; 13. Motor. Detailed Implementation

[0057] To make the technical means, creative features, objectives and effects of this invention easier to understand, the invention will be further described below in conjunction with specific embodiments.

[0058] Please see the appendix Figure 1 - Appendix Figure 3 A macro-micro combined dispersion enhanced liquid-liquid heterogeneous supergravity reactor device includes: a liquid distributor 3 and a liquid distributor 4. One end of the liquid distributor 3 and the liquid distributor 4 are respectively provided with a liquid inlet 1 and a liquid inlet 2. The liquid distributor 3 and the liquid distributor 4 are both provided with liquid distribution branch pipes 5 inside.

[0059] The macro mixer 7 consists of a focusing tube 6, a baffle plate, and a mixing tube.

[0060] The outer shell 9 and the rotating packing 8 are located inside the outer shell 9. The surface of the rotating packing 8 has a serrated protrusion structure. The rotating packing 8 has 4 protrusion structures symmetrically arranged radially at the same position.

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

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

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

[0064] Please see the appendix 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 the appendix Figure 1 The baffles are symmetrically placed inside the mixing tube. The inclination angle of the baffles is 15°-60°, preferably 35°-45°. The baffles are fixed on the inner wall of the mixing tube. The number of baffles is set according to the actual situation, generally 1-3 sets.

[0066] Please see the appendix Figure 1 The main wall of the mixing tube has a corrugated structure and is made of wear-resistant and smooth material, while the inner diameter of the mixing tube remains unchanged.

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

[0068] Please see the appendix Figure 1-2 The rear end of the mixing tube has a variable diameter structure with a smaller inner diameter. The outlet of the mixing tube is aligned with the center of the rotating packing 8. The mixing tube is evenly placed circumferentially in the cavity inside the reactor.

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

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

[0071] This structure facilitates the downward flow of liquid and prevents liquid stagnation.

[0072] Please see the appendix Figure 1 A motor 13 is provided below the outer casing 9. 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 outer casing 9 and is rotatably connected to the outer casing 9. The top end of the rotating shaft 12 is fixedly connected to the bottom of the rotating packing 8.

[0073] Please see the appendix Figure 1 A sealing assembly 11 is installed at the connection 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.

[0074] Example 1

[0075] The device using the present invention and Figure 4The system shown produces epichlorohydrin using dichloropropanol and sodium hydroxide aqueous solution as raw materials. The specific steps and results are as follows:

[0076] A 6% sodium hydroxide aqueous solution was stored in the light phase tank, and chemically pure dichloropropanol liquid was stored in the heavy phase tank. The sodium hydroxide solution had a mass flow rate of 1000 g / min. The dichloropropanol liquid was injected into inlet 2 at a mass flow rate of 170 g / min. The reaction temperature was controlled at 82℃, and the rotary filling rotor speed was 1200 r / min. The product discharge time was recorded, and samples were taken for analysis of the epichlorohydrin content. After 10 minutes, a stable product was obtained, and the epichlorohydrin mass fraction was found to be 99.2%.

[0077] Using the same process and feed rate, with conventional T-type premixed pipe feeding and conventional rotary packing, the stable output product was analyzed to have an epichlorohydrin mass fraction of 92.4%.

[0078] Example 2

[0079] The device using the present invention and Figure 5 The system shown undergoes a concentrated sulfuric acid-catalyzed C4 alkylation reaction. The specific steps and results are as follows:

[0080] The acid feedstock tank contains H2SO4, and the alkane-to-alkene ratio in the gas tank is 30:1. The alkane-to-alkene mixture gas tank is pressurized with nitrogen, and the thermostatic bath containing coolant is started and set to a specified temperature of 4℃. The flow rates of both alkane and H2SO4 are 12 L / h, the acid-to-alkene ratio is 1:1, and the rotational filling rotor speed is 1300 r / min. Then, the liquid mixture enters the stirred tank through the liquid outlet of the centrifugal reactor to continue the reaction. After 15 minutes, the reaction ends, and the liquid mixture automatically separates into two phases. The product is stored in the product tank to obtain alkylated oil. Sample analysis shows that the product yield is 85% and the octane number is 97.

[0081] Using the same reaction process and operating conditions, with conventional T-type premixed tube feed and conventional rotary packing, the product yield was 74% and the octane number was 93.

[0082] Example 3

[0083] The device using the present invention and Figure 5 The system uses trichloroethane and sodium hydroxide aqueous solution as raw materials to produce vinylidene chloride. The specific steps and results are as follows:

[0084] A 0.03 mol / L sodium hydroxide aqueous solution was stored in the aqueous phase tank, and trichloroethane was stored in the oil phase tank. The temperature of the constant temperature bath was controlled, and the temperature change was observed in real time using an electron probe thermometer. When the temperature reached 75°C, the circulation pump was turned on to pump the trichloroethane into the centrifugal reactor to start the reaction. After 10 minutes, the product was condensed and collected to obtain a stable product. The yield of the product was analyzed to be 95.4%.

[0085] Using the same reaction process and operating conditions, with conventional T-type premixed tube feed and conventional rotary packing, the product yield was 85%.

[0086] Those skilled in the art should understand that the discussion of any of the above embodiments is merely exemplary and is not intended to imply that the scope of the invention (including the claims) is limited to these examples; within the framework of the invention, the technical features of the above embodiments or different embodiments can also be combined, the steps can be implemented in any order, and there are many other variations of the different aspects of the invention as described above, which are not provided in the details for the sake of brevity.

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

Claims

1. A macro- and micro-scale combined dispersion-enhanced liquid-liquid heterogeneous hypergravity reactor device, characterized in that, include: Liquid distributor one (3) and liquid distributor two (4), one end of liquid distributor one (3) and liquid distributor two (4) are respectively provided with liquid inlet one (1) and liquid inlet two (2), and liquid distributor one (3) and liquid distributor two (4) are respectively provided with liquid distribution branch pipe (5) inside. The macro mixer (7) consists of a focusing tube (6), a baffle plate, and a mixing tube; The outer shell (9) and the rotating packing (8) are located inside the outer shell (9). The surface of the rotating packing (8) has a serrated protrusion structure. The rotating packing (8) has four protrusion structures symmetrically arranged in the radial direction at the same position. The focusing tube (6) is installed at the outlet of the liquid distribution branch pipe (5). The other end of the focusing tube (6) is connected to the mixing tube. The turbulence baffle is placed symmetrically inside the mixing tube. The rear end of the mixing tube is a variable diameter structure with a smaller inner diameter. The outlet of the mixing tube is aligned with the center of the rotating packing (8). The mixing tube is placed evenly in the circumferential direction in the cavity inside the reactor.

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

3. The macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device according to claim 2, characterized in that, The liquid distribution branch pipes (5) are placed in parallel within the liquid distributor one (3) and the liquid distributor two (4). The number of liquid distribution branch pipes (5) is set according to the actual situation, and is more than two sets.

4. The macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device according to claim 3, characterized in that, The tilt angle of the baffle is between 15° and 60°. The baffle is fixed on the inner wall of the mixing pipe. The number of baffles is set according to the actual situation, ranging from 1 to 3 sets.

5. The macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device according to claim 4, characterized in that, The main wall of the mixing tube has a wavy structure and is made of a wear-resistant and smooth material, while the inner diameter of the mixing tube remains unchanged.

6. The macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device according to claim 1, characterized in that, The bottom of the reactor is an inclined structure with an inclination angle of 10°-75°.

7. The macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device according to claim 1, characterized in that, A motor (13) is provided below the outer shell (9). A rotating shaft (12) is vertically fixed at the output end of the motor (13). The rotating shaft (12) extends into the interior of the outer shell (9) and is rotatably connected to the outer shell (9). The top end of the rotating shaft (12) is fixedly connected to the bottom of the rotating packing (8).

8. The macro-micro combined dispersion enhanced liquid-liquid heterogeneous hypergravity reactor device according to claim 7, characterized in that, A sealing assembly (11) is installed at the connection position between the rotating shaft (12) and the outer casing (9), and a liquid outlet (10) is provided on one side of the bottom of the outer casing (9).

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