A continuous-flow coupling reactor for enhancing mass and heat transfer

Abstract

The present invention discloses a continuous flow coupled reactor for enhancing mass transfer and heat transfer, comprising a shell; a premixing reactor, a shell and tube tubular reactor, and a dynamic mixing enhanced reactor are arranged from top to bottom in the shell; the outlet of the premixing reactor is connected to the distributor of the shell and tube tubular reactor; in the premixing reactor, after the materials are mixed and reacted, the reactants are sent to the feed tubes of the shell and tube tubular reactor; the outlet of the feed tubes is connected to the inlet of the dynamic mixing enhanced reactor, and the dynamic mixing enhanced reactor efficiently mixes the reactants; the outlet of the dynamic mixing enhanced reactor is connected to the reflux tubes of the shell and tube tubular reactor, and the materials discharged from the dynamic mixing enhanced reactor react in the reflux tubes and the circulation tubes, and some of the materials circulate in the circulation tubes; the outlet of the reflux tubes and the upper port of the circulation tubes send the reactants out of the reactor through a liquid collecting tray. The present invention relates to the technical field of reaction system design, and the present invention has continuous and efficient mixing, enhanced mass transfer and heat transfer performance.

Description

Technical Field

[0001] The invention relates to the technical field of reaction system design, in particular to a continuous flow coupled reactor for enhancing mass and heat transfer. Background Art

[0002] Compared to batch reactions, the advantages of continuous flow reactions primarily lie in their efficiency, controllability, and safety. Efficiency: Continuous flow reactions enable a continuous reaction process, thereby improving reactor utilization and production capacity. Materials continuously enter and exit the reactor, allowing the reaction to proceed at a high rate without waiting for reaction completion and reactant cleanup. Controllability: Continuous flow reactions are easier to control and regulate. By adjusting parameters such as feed rate, reaction temperature, and the ratio of reactants, reaction conditions can be more precisely controlled, optimizing the reaction process and improving selectivity and yield. Safety: Continuous flow reactions can reduce process hazards. The reduced liquid holdup and shorter residence time in the reactor minimize heat and pressure buildup, reducing the risk of explosions and accidents. Using continuous flow reactions to intensify chemical processes has become a key development direction in the chemical industry and remains a hot topic of research. Implementation primarily relies on new equipment and processes, including process intensification equipment and process intensification methods. In some cases, these two aspects are interconnected, interpenetrating, and intersecting.

[0003] In the prior art, (1) the reactor of CN202310245903.5 adopts a tubular reactor and an impinging stream reactor, which provides good mass transfer conditions through rapid mixing of the impinging stream reactor. Due to the characteristics of rapid mixing and high-speed flow of reactants, the reaction can occur and reach equilibrium in a short time. The main problem is that the residence time of the impinging stream material is very short. This property, coupled with the difficulty in arranging a multi-stage process, limits the scope of application of a simple impinging stream. For processes limited by equilibrium, although a simple impinging stream can enhance interphase transfer and accelerate it, it is difficult to ensure that the process is completed to the required degree, and the final absorption rate or conversion rate may not reach the expected level. The heat exchange area is small, and it is not suitable for reactions with violent reactions and reactions with relatively slow reaction rates, such as nitration, sulfonation and oxidation of high-concentration sewage. (2) Yang Tao, Yao Wenbo, et al., "Impacting Stream Catalytic Ozone Oxidation-Membrane Filtration Treatment of Emulsified Oil Wastewater", Chemical Environmental Protection, 2022, Vol. 42, No. 6, 678-685, using the impinging stream catalytic ozone oxidation-membrane filtration process to treat emulsified oil wastewater, and the control effect of impinging stream catalytic ozone oxidation on membrane pollution under continuous operation process. The main problems are short reaction residence time, small heat exchange area, and low reaction temperature, which affect the treatment effect. (3) The reactor of CN115041119 A adopts a supergravity reactor with high-quality mass transfer effect: the supergravity reactor improves the mass transfer effect by increasing the contact area and mixing degree between the gas and liquid phases. The main problems are short residence time, large reactor liquid holding capacity, small heat exchange area, and still have safety and environmental protection risks. (5) The reactor of CN 102432410 B realizes pipeline continuous production. The main problem is low efficiency of the parallel flow reaction stage, and production efficiency needs to be improved. (6) The main problem with the reactor in CN 107793316 B is that the microreactor channel is relatively thin, easily clogged, and inconvenient to maintain. In addition, the residence time is short, which is not conducive to reactions with relatively slow reaction rates. (7) The reactor in CN 104710062A uses ultrasound to introduce mechanical vibration, thereby generating localized violent eddies and shear forces, further promoting the mixing of the reactants and increasing the interfacial reaction rate. Ultrasonic waves can also destroy the aggregation of solid particles, making them easier to react. The main problem is that the processing time is short, making it unsuitable for relatively slow reactions and exothermic or endothermic reactions.

[0004] Existing continuous flow technologies mostly adopt the form of combining two or three reactors in parallel. The heat transfer distance is long, the heat exchange area is small, the heat transfer efficiency is low, the local reactor may have high temperature, the residence time is short, and the reaction level efficiency is low. Especially for fast and highly exothermic reaction systems, there are safety hazards. It is particularly important to make full use of the respective advantages of various enhanced mass transfer and heat transfer reactors and develop enhanced mass transfer and heat transfer continuous flow coupled reactors. Summary of the Invention

[0005] The present invention aims to address the problems of long heat transfer distance, small heat exchange area, low heat transfer efficiency, possibility of high temperature in local reactors, short residence time, low reaction stage efficiency, and especially safety hazards in rapid and highly exothermic reaction systems in existing reactors. The present invention proposes an enhanced mass transfer and heat transfer continuous flow coupled reactor. By rationally optimizing the premixing reactor, the tube-in-tube reactor, the dynamic mixing enhanced reactor and the shell, the reactor is ensured to have efficient mixing, self-absorption circulation, efficient mass transfer and heat transfer performance, thereby improving the reaction stage efficiency, conversion rate and yield, realizing isothermal continuous reaction, and being able to rationally set the reactor heat exchange area to eliminate safety hazards.

[0006] In order to achieve the above object, the present invention adopts the following technical solutions:

[0007] A continuous flow coupled reactor for enhancing mass and heat transfer comprises a shell and a premixing reactor, a shell-and-tube tubular reactor and a dynamic mixing enhanced reactor connected together at the upper and lower parts thereof, a first material inlet and a second material inlet connected to the premixing reactor through the shell, a system material outlet connected to the shell and tube tubular reactor through the shell, a heat exchange medium inlet disposed at the lower part of the shell through the shell, and a heat exchange medium outlet disposed at the upper part of the shell through the shell.

[0008] Furthermore, the premixing reactor is provided with the first material inlet, the second material inlet and a premixing reactor discharge port or a tubular reactor distributor;

[0009] The premixing reactor can introduce materials through at least the first material inlet and the second material inlet. The direction of the first material inlet and the direction of the second material inlet are axially opposite, tangentially opposite, or tangentially the same, so as to facilitate collision and swirl, generate cavitation, achieve micro-nano mixing, and enhance reaction.

[0010] Furthermore, the premixing reactor may be provided with at least one ultrasonic feeder, which is placed in the middle or upper middle portion of the premixing reactor to assist in strengthening the mixing reaction process;

[0011] The ultrasonic frequency range of the ultrasonic feeder is 18,000 Hz to 5 MHz.

[0012] Furthermore, the tube-in-tube reactor is provided with feed tubes, reflux tubes and circulation tubes;

[0013] The feed tubes are located in the middle of the tube-type reactor, the reflux tubes are located outside the circulation tubes, and the circulation tubes are located between the reflux tubes and the feed tubes;

[0014] The number of the feed tube is at least one, and the number of the reflux tube and the circulation tube is at least two;

[0015] At least one of the feed pipes is connected to the premixing reactor outlet of the premixing reactor.

[0016] Furthermore, the dynamic mixing enhanced reactor comprises a dynamic mixing enhanced reactor feed port and a circulation tube feed port, a dynamic mixing enhanced reactor discharge port, a rotating shaft, a high-speed rotating component and a motor;

[0017] The feed port of the dynamic mixing enhanced reactor is connected to the feed tube, the material port below the reflux tube and the circulation tube is connected to the dynamic mixing enhanced reactor, the discharge port of the dynamic mixing enhanced reactor is connected to the reflux tube, the material discharged from the dynamic mixing enhanced reactor reacts in the reflux tube and the circulation tube, and part of the material circulates in the circulation tube, and the reflux tube outlet and the upper port of the circulation tube discharge the final material from the system material outlet through the liquid collection tray;

[0018] The feed inlet of the dynamic mixing enhanced reactor enters the high-speed rotating component vertically from top to bottom from the center of the high-speed rotating component, the circulation tube feed inlet is concentrated at the edge of the center of the high-speed rotating component, the feed inlet of the dynamic mixing enhanced reactor and the circulation tube feed inlet have a certain gap with the high-speed rotating component, the discharge port of the dynamic mixing enhanced reactor is located on both sides of the feed inlet of the dynamic mixing enhanced reactor and is connected to the reflux tube, the motor is located outside the bottom of the shell, vertically opposite to the center of the dynamic mixing enhanced reactor, and adopts packing seal or mechanical seal or dry gas seal or magnetic coupling, the motor relies on electricity to drive the rotating shaft to drive the high-speed rotating component located at the center of the dynamic mixing enhanced reactor to rotate at high speed, and under the action of centrifugal force, radial diffusion and mixing are realized, so as to achieve high material Mixing, enhancing mass and heat transfer, and intensifying reactions;

[0019] At least one group of discharge ports of the dynamic mixing enhanced reactor is connected to the reflux tubes of the tube-in-tube reactor;

[0020] The circulation tubes of at least one group of the tube-in-tube reactors are connected to the discharge port of the dynamic mixing enhanced reactor.

[0021] Furthermore, the components placed in the shell, including the premixing reactor, the tubular reactor, and the dynamic mixing enhanced reactor, achieve heat exchange through the heat exchange medium inlet located at the lower part of the shell and the heat exchange medium outlet located at the upper part of the shell.

[0022] Furthermore, the premixing reactor can produce efficient dispersion and cavitation;

[0023] The microscopic size of the premixing reactor is between 0.5 microns and 2000 microns.

[0024] Furthermore, at least one feed tube can be arranged between the tube-in-tube reactor and the dynamic mixing enhanced reactor, connected to the feed port of the dynamic mixing enhanced reactor, and fed into the high-speed rotating component of the dynamic mixing enhanced reactor.

[0025] Furthermore, at least one group of circulation tubes can be arranged between the tube-in-tube reactor and the dynamic mixing enhanced reactor and connected to the dynamic mixing enhanced reactor, and the self-priming circulation reaction can be achieved by utilizing the rotation of the high-speed rotating component of the dynamic mixing enhanced reactor.

[0026] Furthermore, the microscopic size of the dynamic mixing enhanced reactor is between 0.5 microns and 3000 microns, and the rotation speed of the rotating component is between 500 rpm and 5000 rpm.

[0027] Furthermore, the characteristic diameter ratio of the shell-and-tube tubular reactor is between 1:100 and 1:5;

[0028] The tubular reactor is provided with fillers and static mixing components to facilitate interface renewal, heterogeneous catalysis, and prolonged residence time.

[0029] Further, the ratio of the residence time of the fluid in the premixing reactor to the residence time of the fluid in the shell-and-tube tubular reactor is between 1:200 and 1:50;

[0030] The ratio of the residence time of the fluid in the tubular reactor to the residence time of the fluid in the dynamic mixing enhanced reactor is between 50:1 and 300:1.

[0031] Compared with the prior art, the present invention has the following advantages:

[0032] The present invention provides a continuous flow coupled reactor for enhancing mass transfer and heat transfer. The reactor is based on the theoretical basis of impinging flow / swirl, ultrasound, shell-and-tube reactors, and centrifugal rotation to accelerate and enhance mass transfer and heat transfer, combined with the heat transfer characteristics of shell-and-tube heat exchangers, and utilizes the shell-and-tube reactor to extend the reaction time, accelerate the renewal of the interface, and increase the heat exchange area. The reactor is rationally optimized for the premixing reactor, the shell-and-tube reactor, the dynamic mixing enhanced reactor, and the shell. The reactor is subjected to a strong dynamic rotation stirring centrifugal force self-priming circulation technology to ensure full mixing of materials and forced circulation without dead angles. The materials form an inner bottom and outer top "magnetic field type" self-priming internal circulation in the reactor, which greatly improves the mass transfer and heat transfer efficiency, ensures that heat can be exchanged through the shell-and-tube surface and the shell side under any circumstances, avoids the possibility of overall or local high temperature, ensures that the reactor has efficient mixing, mass transfer and heat transfer performance, improves the reaction stage efficiency, conversion rate, and yield, realizes isothermal continuous reaction, and can rationally set the heat exchange area of the reactor, fundamentally guarantees safety, and eliminates safety hazards. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] The accompanying drawings, which constitute part of the present invention, are provided to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the accompanying drawings:

[0034] Figure 1 This is an overall schematic diagram of a continuous flow coupled reactor for enhancing mass and heat transfer according to an embodiment of the present invention;

[0035] Figure 2 The embodiment of the present invention Figure 1 AA cross-section of

[0036] Figure 3 The embodiment of the present invention Figure 1 BB cross-section diagram;

[0037] Figure 4 The embodiment of the present invention Figure 1 CC cross-section diagram;

[0038] Description of reference numerals:

[0039] 1. Shell; 2. Premixing reactor; 201. First material inlet; 202. Second material inlet; 203. Discharge port of premixing reactor / the tubular reactor distributor; 204. Ultrasonic feeder; 3. Shell and tube tubular reactor; 301. Feed shell and tube tubular reactor; 302. Reflux shell and tube tubular reactor; 303. Circulation shell and tube tubular reactor; 4. Dynamic mixing enhanced reactor; 401. Feed port of dynamic mixing enhanced reactor; 402. Circulation shell and tube feed port of dynamic mixing enhanced reactor; 403. Discharge port of dynamic mixing enhanced reactor; 404. Rotating shaft; 405. High-speed rotating component; 406. Motor; 5. System material outlet; 6. Heat exchange medium inlet; 7. Heat exchange medium outlet; 8. Liquid collection tray. DETAILED DESCRIPTION

[0040] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments may be combined with each other.

[0041] In the description of the present invention, it should be noted that the terms "upper," "lower," "inner," and "back" and other terms indicating orientations or positional relationships are based on the orientations or positional relationships shown in the accompanying drawings and are intended solely to facilitate and simplify the description of the present invention. They are not intended to indicate or imply that the devices or components referred to must have, be constructed, or operate in a specific orientation, and therefore should not be construed as limitations on the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0042] The present invention will be described in detail below with reference to the accompanying drawings and in conjunction with embodiments.

[0043] Example 1

[0044] This embodiment relates to a continuous flow coupled reactor that enhances mass and heat transfer, Figure 1-4 As shown, it specifically includes a shell 1 and a premixing reactor 2, a shell-and-tube tubular reactor 3 and a dynamic mixing enhanced reactor 4 connected together in the upper and lower parts thereof, a first material inlet 201 and a second material inlet 202 connected to the premixing reactor 2 through the shell 1, a system material outlet 5 connected to the shell 1 and the shell-and-tube tubular reactor 3, a heat exchange medium inlet 6 located at the lower part of the shell 1 through the shell 1 and a heat exchange medium outlet 7 located at the upper part of the shell 1 through the shell 1.

[0045] The premixing reactor 2 is provided with a first material inlet 201, a second material inlet 202 and a premixing reactor discharge port / the tubular reactor distributor 203; the premixing reactor 2 can introduce materials through at least the first material inlet 201 and the second material inlet 202. The orientation of the first material inlet 201 and the orientation of the second material inlet 202 can be axially opposite, tangentially opposite, or tangentially the same, thereby causing collision and swirl to generate cavitation, achieve micro-nano mixing, and enhance the reaction.

[0046] The premixing reactor 2 may be provided with at least one ultrasonic feeder 204, which is placed in the middle or upper middle portion of the premixing reactor 2 to assist in enhancing the mixing reaction process; the ultrasonic frequency range of the ultrasonic feeder 204 is 18,000 Hz-5 MHz.

[0047] The shell and tube reactor 3 is provided with a feed shell and tube 301, a reflux shell and tube 302 and a circulation shell and tube 303; the feed shell and tube 301 is located in the middle of the shell and tube reactor 3, the reflux shell and tube 302 is located outside the circulation shell and tube 303, and the circulation shell and tube 303 is located between the reflux shell and tube 302 and the feed shell and tube 301; the number of the feed shell and tube 301 is at least one, and the number of the reflux shell and tube 302 and the circulation shell and tube 303 is at least two; at least one feed shell and tube 301 is connected to the premixing reactor discharge port 203 of the premixing reactor 2; the dynamic mixing enhanced reactor 4 includes a dynamic mixing enhanced reactor feed port 401 and a circulation shell and tube feed port 402, a dynamic mixing enhanced reactor discharge port 403, a rotating shaft 404, a high-speed rotating component 405 and a motor 406.

[0048] The feed inlet 401 of the dynamic mixing enhanced reactor is connected to the feed tubular reactor 301, the material port below the reflux tubular reactor 302 and the circulation tubular reactor 303 is connected to the dynamic mixing enhanced reactor, and the outlet 403 of the dynamic mixing enhanced reactor is connected to the reflux tubular reactor 302 of the tubular reactor. The material discharged from the dynamic mixing enhanced reactor reacts in the reflux tubular reactor 302 and the circulation tubular reactor 303, and part of the material circulates in the circulation tubular reactor 303. The outlet of the reflux tubular reactor 302 and the upper port of the circulation tubular reactor 303 discharge the final material from the system material outlet 5 through the liquid collecting tray 8.

[0049] The feed inlet 401 of the dynamic mixing enhanced reactor enters the high-speed rotating component 405 vertically from top to bottom through the center of the high-speed rotating component 405, the circulation tube feed inlet 402 is concentrated at the edge of the center of the high-speed rotating component 405, and there is a certain gap between the feed inlet 401 and the circulation tube feed inlet 402 of the dynamic mixing enhanced reactor and the high-speed rotating component 405. The discharge port 403 of the dynamic mixing enhanced reactor is located on both sides of the dynamic mixing enhanced reactor 401 and is connected to the reflux tube tubular reactor 302. The motor 406 is located outside the bottom of the shell 1, vertically opposite to the center of the dynamic mixing enhanced reactor 4, and adopts packing seal, mechanical seal, dry gas seal or magnetic coupling. The motor 406 relies on electricity to drive the rotating shaft 404 to drive the high-speed rotating component 405 located at the center of the dynamic mixing enhanced reactor to rotate at high speed. Under the action of centrifugal force, radial diffusion and mixing are achieved, efficient mixing of materials is achieved, mass transfer and heat transfer are enhanced, and reaction is enhanced; at least one group of dynamic mixing enhanced reactor discharge ports 403 is connected to the reflux tube 302 of the tube tubular reactor 3.

[0050] The circulation tubes 303 of at least one group of tube-in-tube reactors 3 are connected 403 to the dynamic mixing enhanced reactor.

[0051] The premixing reactor 2, the shell-and-tube reactor 3, and the dynamic mixing enhanced reactor 4 of each component placed in the shell 1 realize heat exchange through a heat exchange medium inlet 6 located at the lower part of the shell 1 and a heat exchange medium outlet 7 located at the upper part of the shell 1.

[0052] The premixing reactor 2 can produce efficient dispersion and cavitation; the microscopic size of the premixing reactor 2 is between 0.5 microns and 2000 microns.

[0053] At least one dynamic reactor feed tube 301 can be set between the tubular reactor 3 and the dynamic mixing enhanced reactor 4 to be connected to the dynamic mixing enhanced reactor feed port 401 of the dynamic mixing enhanced reactor 4 and fed into the high-speed rotating component 405 of the dynamic mixing enhanced reactor 4.

[0054] At least one group of circulating tubular reactors 303 can be arranged between the tubular reactor 3 and the dynamic mixing enhanced reactor 4 and connected to the dynamic mixing enhanced reactor 4, and the self-priming circulating reaction can be realized by the rotation of the high-speed rotating component 405 of the dynamic mixing enhanced reactor 4.

[0055] The microscopic size of the dynamic mixing enhanced reactor 4 is between 0.5 microns and 3000 microns, and the rotation speed of the rotating component is between 500 rpm and 5000 rpm.

[0056] The characteristic diameter ratio of the shell-and-tube tubular reactor 3 is between 1:100 and 1:5.

[0057] The tubular reactor 3 is provided with fillers and static mixing components to facilitate interface renewal, heterogeneous catalysis, and prolonged residence time.

[0058] The ratio of the residence time of the fluid in the premixing reactor 2 to the residence time of the fluid in the shell-and-tube tubular reactor 3 is between 1:200 and 1:50; the ratio of the residence time of the fluid in the shell-and-tube tubular reactor 3 to the residence time of the fluid in the dynamic mixing enhanced reactor 4 is between 50:1 and 300:1.

[0059] Example 2

[0060] The mass transfer and heat transfer enhanced continuous flow coupled reactor of the present invention is used for the continuous synthesis of nitrochlorobenzene.

[0061] Using chlorobenzene (CP, 99% by mass), concentrated sulfuric acid (CP, 98% by mass), and nitric acid (CP, 65%-68% by mass) as raw materials, the present invention employs a continuous flow coupled reactor with enhanced mass and heat transfer to continuously synthesize nitrochlorobenzene. The sulfuric acid and nitric acid are first circulated within the continuous flow nitration reactor, and the chlorobenzene is then preheated and continuously and stably introduced into the reactor. The flow and reaction conditions are precisely metered and controlled. Under conditions of a residence time of 70 seconds, a temperature of 80°C, a mixed acid ratio (molar ratio of nitric acid to sulfuric acid) of 1:1.5, a phase ratio (molar ratio of nitric acid to chlorobenzene) of 1:1, an ultrasonic frequency of 26,000 Hz, a rotational speed of 3,000 rpm for the rotating components of the dynamic mixing enhanced reactor, and a slight negative pressure in the reactor, the ortho-to ... The nitration of aromatic compounds is a rapid, highly exothermic reaction. Using this nitration process, the heat of reaction is rapidly removed by cooling water through the tube walls, reducing potential risks associated with intermittent operation. Compared to conventional kettle processes, continuous nitration in the continuous flow reactor of the present invention is safer and more efficient.

[0062] Example 3

[0063] Pretreatment of cimetidine pharmaceutical wastewater using the enhanced mass transfer and heat transfer continuous flow coupled reactor of the present invention

[0064] Cimetidine pharmaceutical wastewater has high COD and complex components. The present invention utilizes a continuous flow coupled reactor with enhanced mass and heat transfer, pre-treating the wastewater with a Fenton reagent. The wastewater is first circulated within the reactor, and preheated FeSO4, along with water and wastewater, enters the reactor continuously and stably, precisely metering and controlling the flow and reaction conditions. The optimal reaction conditions are: an H2O2 mass concentration of 3000 mg / L, an FeSO4 mass concentration of 750 mg / L, an ultrasonic frequency of 20,000 Hz, a rotational speed of 3000 rpm for the rotating components of the dynamic mixing enhanced reactor, a slightly negative reactor pressure, an oxidation time of 80 seconds, a pH of 3.5, a reaction temperature of 75°C, and a COD removal rate exceeding 56%.

[0065] Example 4

[0066] Pretreatment of glyphosate production wastewater using the enhanced mass transfer and heat transfer continuous flow coupled reactor of the present invention

[0067] The present invention utilizes a continuous flow coupled reactor with enhanced mass and heat transfer, using a catalytic wet oxidation method to pretreat glyphosate production wastewater using copper sulfate and zinc nitrate solutions as catalysts. The process raw water contains: COD 46,300 mg / L, total phosphorus 6,800 mg / L, inorganic phosphorus -, and a pH of 8.0. The wastewater is adjusted to a pH of 8.5 with a 1 mol / L NaOH solution and fed into a preheater via a high-pressure metering pump. A valve regulates the air pressure in the high-pressure cylinder to 3 MPa. A mass controller controls the air flow rate, mixing it with the wastewater in the preheater. The mixture is heated to 220°C by an automatic temperature-controlled electric heater and then fed into the reactor for oxidation. The treated water mixture is condensed in a condenser, separated in a gas-liquid separator, and then discharged separately. The wastewater resides in the reactor for 100 seconds, the ultrasonic frequency is 28,000 Hz, and the rotating components of the dynamic mixing enhanced reactor rotate at 3,500 rpm. The water quality analysis results after catalytic wet oxidation of wastewater were COD 7600mg / L, total phosphorus 6800mg / L, inorganic phosphorus 6500mg / L, COD removal rate 85%, and organic phosphorus removal rate 99.6%.

Claims

1. A continuous flow coupled reactor for enhanced mass and heat transfer, characterized in that: The invention comprises a shell (1) and a premixing reactor (2), a shell-and-tube tubular reactor (3) and a dynamic mixing enhanced reactor (4) connected together at the upper and lower parts thereof, a first material inlet (201) and a second material inlet (202) connected to the premixing reactor (2) through the shell (1), a system material outlet (5) connected to the shell (1) and the shell-and-tube tubular reactor (3), a heat exchange medium inlet (6) located at the lower part of the shell (1) through the shell (1), and a heat exchange medium outlet (7) located at the upper part of the shell (1) through the shell (1); The tube-and-tube reactor (3) is provided with a feed tube (301), a reflux tube (302) and a circulation tube (303); The dynamic mixing and intensifying reactor (4) comprises a dynamic mixing and intensifying reactor feed port (401), a circulating tube feed port (402), a dynamic mixing and intensifying reactor discharge port (403), a rotating shaft (404), a high-speed rotating component (405), and a motor (406); The premixing reactor (2), the tubular reactor (3), and the dynamic mixing enhanced reactor (4) disposed in the shell (1) realize heat exchange through the heat exchange medium inlet (6) disposed at the lower portion of the shell (1) and the heat exchange medium outlet (7) disposed at the upper portion of the shell (1) through the shell (1); At least one group of the circulation tubes (303) is connected to the dynamic mixing enhanced reactor (4), and a self-priming circulation reaction is achieved by utilizing the rotation of the high-speed rotating component (405) of the dynamic mixing enhanced reactor (4); The premixing reactor (2) is provided with the first material inlet (201), the second material inlet (202) and a premixing reactor discharge port (203); The premixing reactor (2) can be used to introduce materials through at least the first material inlet (201) and the second material inlet (202), and the direction of the first material inlet (201) and the direction of the second material inlet (202) are axially opposite, tangentially opposite, or tangentially the same; The premixing reactor (2) is provided with at least one ultrasonic feeder (204), and the ultrasonic feeder (204) is placed in the middle or upper middle portion of the premixing reactor (2) to assist in strengthening the mixing reaction process; The feed tubes (301) are located in the middle of the tube-type reactor (3), the reflux tubes (302) are located outside the circulation tubes (303), and the circulation tubes (303) are located between the reflux tubes (302) and the feed tubes (301); The number of the feed tube (301) is at least one, and the number of the reflux tube (302) and the circulation tube (303) is at least two; At least one of the feed tube arrays (301) is connected to the premixing reactor outlet (203) of the premixing reactor (2); The feed port (401) of the dynamic mixing enhanced reactor is connected to the feed tube (301), the material ports below the reflux tube (302) and the circulation tube (303) are in communication with the dynamic mixing enhanced reactor, and the discharge port (403) of the dynamic mixing enhanced reactor is in communication with the reflux tube (302). The material discharged from the dynamic mixing enhanced reactor reacts in the reflux tube (302) and the circulation tube (303), and part of the material circulates in the circulation tube (303). The liquid collecting tray (8) connected to the outlet of the reflux tube (302) and the upper port of the circulation tube (303) discharges the final material from the system material outlet (5).

2. The continuous flow coupled reactor for enhanced mass and heat transfer according to claim 1, characterized in that: The feed inlet (401) of the dynamic mixing enhanced reactor enters the high-speed rotating component (405) vertically from the center of the high-speed rotating component (405) from top to bottom, the circulation tube feed inlet (402) is concentrated at the edge of the center of the high-speed rotating component (405), the feed inlet (401) of the dynamic mixing enhanced reactor and the circulation tube feed inlet (402) are spaced a certain distance from the high-speed rotating component (405), the discharge port (403) of the dynamic mixing enhanced reactor is located on both sides of the feed inlet (401) of the dynamic mixing enhanced reactor and is connected to the reflux tube (302), the motor (406) is located outside the bottom of the shell (1), vertically opposite to the center of the dynamic mixing enhanced reactor (4), and adopts packing seal, mechanical seal, dry gas seal or magnetic coupling, the motor (406) relies on electricity to drive the rotating shaft (404) to drive the high-speed rotating component (405) located at the center of the dynamic mixing enhanced reactor to rotate at high speed.

3. The continuous flow coupled reactor with enhanced mass and heat transfer according to claim 1, characterized in that: Fillers and static mixing components are provided inside the tubular reactor (3).

4. The continuous flow coupled reactor with enhanced mass and heat transfer according to claim 1, characterized in that: The ratio of the residence time of the fluid in the premixing reactor (2) to the residence time of the fluid in the shell-and-tube tubular reactor (3) is between 1:200 and 1:50.

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