CN113877513B - Reaction kettle between hypergravity films - Google Patents

Reaction kettle between hypergravity films Download PDF

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Publication number
CN113877513B
CN113877513B CN202111354111.9A CN202111354111A CN113877513B CN 113877513 B CN113877513 B CN 113877513B CN 202111354111 A CN202111354111 A CN 202111354111A CN 113877513 B CN113877513 B CN 113877513B
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rotor
liquid
wall
impeller
gas
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CN113877513A (en
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张昕伟
解家杰
黄琳
肖杨
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Chengdu Alite Building Materials Co ltd
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Chengdu Alite Building Materials Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/28—Moving reactors, e.g. rotary drums
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B01J19/0073—Sealings
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/008—Feed or outlet control devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/02—Feed or outlet devices; Feed or outlet control devices for feeding measured, i.e. prescribed quantities of reagents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00164—Controlling or regulating processes controlling the flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0801—Controlling the process
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Abstract

The invention discloses a reaction kettle between hypergravity films, which comprises an outer shell, a liquid reactant feeding pipe and a gas reactant feeding pipe, wherein a stirrer is arranged in the outer shell and comprises a rotor with a hollow cylindrical structure, and a plurality of through holes are formed in the circumferential outer wall of the rotor; the gas reactant feeding pipe is arranged in the rotor; the edge of the outer wall of the rotor is provided with a first guide impeller, a packing layer and a second guide impeller in sequence outwards; be provided with the drive arrangement who is used for driving agitator pivoted on the shell body, liquid, gas in this scheme's reation kettle are dispersed, broken by first impeller, packing layer and second impeller, form very big, constantly renew surface area, and tortuous runner has aggravated the renewal of extremely thin and surface of liquid, has formed ultra-thin gas-liquid film, and extremely thin gas-liquid film has evenly formed ultra-thin gas-liquid film on the convex and concave surface after the impeller of second simultaneously, makes it form the reaction between the membrane.

Description

Reaction kettle between hypergravity films
Technical Field
The invention relates to the technical field of hypergravity engineering, in particular to a hypergravity reaction kettle between films.
Background
The basic principle of the supergravity engineering technology is to strengthen the relative speed and mutual contact between phases by utilizing the unique flow behavior of a multiphase flow system under the supergravity condition, thereby realizing the efficient mass and heat transfer process and chemical reaction process. The hypergravity is obtained mainly by rotating the whole or part of the equipment to form a centrifugal force field, and the related multiphase flow system mainly comprises a gas-solid system and a gas-liquid system. Centrifugal force fields (hypergravity fields) are used for phase separation, both in everyday life and in industrial applications, for a considerable history.
The packed bed in the reaction kettle in the prior art is easy to be blocked by reactants, so that the reaction kettle cannot run for a long time, the overhaul time is prolonged, the production efficiency of the reaction kettle is reduced, and extra manpower and material resources are also required to maintain the normal running of equipment, so that the production cost is increased.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a reaction kettle between hypergravity films, which solves the problems of low production efficiency and high production cost caused by the fact that a packed bed in the existing reaction kettle is easily blocked by reactants.
In order to achieve the above purpose, the invention adopts the following technical scheme:
the reactor comprises an outer shell, a liquid reactant feeding pipe and a gas reactant feeding pipe; the stirrer is arranged in the outer shell and comprises a rotor with a hollow cylindrical structure, and a plurality of through holes are formed in the outer wall of the circumference of the rotor; the gas reactant feeding pipe is arranged in the rotor; the edge of the outer wall of the rotor is provided with a first guide impeller, a packing layer and a second guide impeller in sequence outwards; the first impeller comprises a plurality of first blades with a C-shaped cross section and uniformly arranged at intervals along the circumferential outer wall of the rotor; one end of each first blade is fixedly connected with the outer wall of the rotor, and the length direction of each first blade is in the same direction as the length direction of the rotor;
the packing layer is of a porous hollow cylindrical structure, and a gap for a liquid reactant feeding pipe to pass through is arranged between the inner wall of the packing layer and the outer wall of the first guide vane wheel;
the second impeller is sleeved on the circumferential outer wall of the packing layer and comprises a plurality of second blades with S-shaped cross sections and uniformly distributed along the circumferential outer wall of the packing layer at annular intervals, and the length direction of the second blades is the same as the length direction of the rotor;
the axis of the rotor, the axis of the first impeller, the axis of the packing layer and the axis of the second impeller are all coincident; and the driving device is used for driving the stirrer to rotate.
The basic principle of the scheme is as follows: the driving device realizes centrifugal rotation of the stirrer, and simultaneously, a gas reactant enters the rotor through a gas reactant feeding pipe, and a liquid reactant enters a gap between the inner wall of the packing layer and the outer wall of the first guide vane wheel through a liquid reactant feeding pipe; under the action of high-speed centrifugation and gas pressure, gas flows from the interior of a rotor to a first guide impeller, a packing layer and a second guide impeller in sequence, and when passing through the first guide impeller and the second guide impeller, the gas is accelerated to pass through, and because of the arrangement of the shape of the blades in the two guide impellers, the gas rapidly flows on the convex surface points of the two guide impellers to form a limit gas film; under the action of high-speed centrifugation and liquid pressure, the liquid flows through the packing layer and the second guide vane wheel, and forms an ultrathin gas-liquid film after contacting with a limiting gas film; in the process, the liquid and the gas are dispersed and crushed by the first impeller, the packing layer and the second impeller to form a large surface area which is continuously updated, and the tortuous flow passage exacerbates the ultrathin liquid and the surface updating. Thus, the stirrer has excellent mass transfer and reaction conditions, and the gas and liquid are controlled automatically to form ultrathin gas-liquid film, and the ultrathin gas-liquid film is formed on the convex and concave surfaces after passing through the second guide vane wheel to form ultrathin gas-liquid film for reaction between the films. Meanwhile, the speed between mass transfer objects can be controlled between 7 m/s-12 m/s after the gas-liquid phase passes through the first impeller and the second impeller, and vortex-shaped fluid is formed by the concave surfaces of the first blade and the second blade, so that fine particle products are thrown out by the second blade, coarse particle products move downwards from the vortex center inside the rotor, the non-blocking state is achieved, and the particle size of reaction products is controllable. The whole reaction kettle is not easy to be blocked by reactants, the condition that the reaction kettle cannot run for a long time is avoided, the reaction kettle can run for a long time, the overhaul time is shortened, the production efficiency is improved, and the production cost is reduced.
Further, as the concrete setting mode of liquid reactant inlet pipe, the quantity of liquid reactant inlet pipe is many, and many liquid reactant inlet pipe annular interval evenly set up in the clearance between the inner wall of packing layer and the outer wall of first impeller, and the bottom of every liquid reactant inlet pipe is seal structure, all is provided with a liquid outlet on the outer wall of every liquid reactant inlet pipe, and the direction of liquid outlet is the tangential direction of liquid reactant inlet pipe, and the length direction of export is the length direction syntropy of liquid reactant inlet pipe. The direction of the liquid outlet is the tangential direction of the liquid reactant feeding pipe, so that a narrow pipe effect is generated when liquid flows out from the liquid reactant feeding pipe, the initial speed of liquid outflow is increased, an ultrathin gas-liquid film is easier to form, the reaction between the liquid and the gas is accelerated, and the reaction efficiency is improved.
Further, as a specific setting mode of the gas reactant feeding pipe, the bottom of the gas reactant feeding pipe is of a sealing structure, a plurality of air outlet holes are uniformly formed in the outer wall of the gas reactant feeding pipe at intervals, and the direction of each air outlet hole is the tangential direction of the gas reactant feeding pipe. The gas flows out from the gas outlet hole, the initial speed of the gas is high due to the narrow pipe effect, and the gas is accelerated again when passing through the first guide vane wheel, so that the gas rapidly flows on the convex surface point of the first vane to form a limit gas film.
Further, in order to make the temperature in the outer shell constant and ensure that the reaction temperature condition of the product is met, a cooling device is further arranged in the outer shell, the cooling device comprises a cooling pipe with a spiral structure, and a cooling liquid inlet and a cooling liquid outlet which are respectively arranged at two sides of the outer shell, and the cooling liquid inlet and the cooling liquid outlet are respectively communicated with two ends of the cooling pipe; the stirrer is arranged in the cooling pipe.
Further, in order to realize synchronous rotation of the rotor, the top of the first impeller, the top of the packing layer and the second impeller, the stirrer further comprises a mounting plate, wherein the rotor, the top of the first impeller, the top of the packing layer and the top of the second impeller are fixedly connected with the lower end face of the mounting plate, and a plurality of notches for allowing the gas reactant feed pipe to pass through the mounting plate and be located in the rotor and for allowing the liquid reactant feed pipe to pass through the mounting plate and be located in the gap are formed in the mounting plate.
Further, the stirrer further comprises a stirring shaft, one end of the stirring shaft penetrates through the outer shell and is fixedly connected with the inner wall of the rotor, and the other end of the stirring shaft is positioned outside the outer shell and is connected with the driving device.
Further, in order to ensure the sealing performance of the outer shell, the leakage of the product from the outer shell is avoided, and a dynamic seal bearing is arranged at the joint of the stirring shaft and the outer shell.
Further, as a specific embodiment of the driving device, the driving device comprises a variable frequency motor, and a driving belt pulley is arranged on an output shaft of the variable frequency motor; the end part of the stirring shaft positioned outside the outer shell is provided with a driven belt pulley, and the driving belt pulley drives the driven belt pulley to rotate through a belt.
Further, be provided with the resultant discharge gate rather than inside intercommunication on the shell body bottom lateral wall, the shell body top is provided with sealed lid, and the setting of resultant discharge gate is convenient takes out the production in the shell body.
The beneficial effects of the invention are as follows: 1. the liquid and gas in the reaction kettle are dispersed and crushed by the first guide impeller, the packing layer and the second guide impeller to form a very large and continuously updated surface area, the tortuous flow passage aggravates the update of the extremely thin liquid and the surface to form an ultrathin gas-liquid film, and simultaneously, the extremely thin gas-liquid film uniformly forms an ultrathin gas-liquid film on the convex and concave surfaces after passing through the second guide impeller, so that the ultrathin gas-liquid film forms a reaction between films, and no substance participates in the reaction due to no mass transfer condition outside the gas-liquid film, thereby the reaction is instantly completed between films and the reaction efficiency is quickened.
2. According to the scheme, the driving device can drive the stirrer to centrifugally rotate at different speeds, vortex-shaped fluid is formed on the concave surfaces of the first blade and the second blade, so that fine grain products are thrown out by the second blade, coarse grain products move downwards from the vortex center inside the rotor, a non-blocking state is achieved, and the particle size of reaction products is controllable. Therefore, the whole reaction kettle is not easy to be blocked by reactants, the condition that the reaction kettle cannot run for a long time is avoided, the reaction kettle can run for a long time, the overhaul time is shortened, the production efficiency is improved, and the production cost is reduced.
Drawings
FIG. 1 is a schematic structural diagram of a reactor between hypergravity membranes.
FIG. 2 is an enlarged schematic view of the liquid reactant feed tube.
FIG. 3 is an enlarged schematic view of the structure of the gas reactant feed pipe.
Fig. 4 is a schematic cross-sectional structure of the stirrer.
Fig. 5 is a schematic perspective view of a stirrer.
Wherein, 1, the outer shell; 2. a liquid reactant feed tube; 201. a liquid outlet; 3. a gaseous reactant feed tube; 301. an air outlet hole; 4. a stirrer; 401. a stirring shaft; 5. a rotor; 6. a first inducer; 601. a first blade; 7. a filler layer; 8. a second inducer; 801. a second blade; 9. a cooling tube; 10. a cooling liquid inlet; 11. a cooling liquid outlet; 12. a mounting plate; 13. a dynamic seal bearing; 14. a variable frequency motor; 15. a driving pulley; 16. a driven pulley; 17. a product discharge port; 18. sealing cover.
Detailed Description
The following description of the embodiments of the present invention is provided to facilitate understanding of the present invention by those skilled in the art, but it should be understood that the present invention is not limited to the scope of the embodiments, and all the inventions which make use of the inventive concept are protected by the spirit and scope of the present invention as defined and defined in the appended claims to those skilled in the art.
As shown in fig. 1 to 5, the invention provides a reactor between hypergravity films, which comprises an outer shell 1, a liquid reactant feeding pipe 2 and a gas reactant feeding pipe 3. The stirrer 4 is arranged in the outer shell 1, the stirrer 4 comprises a rotor 5 with a hollow cylindrical structure, and a plurality of through holes are formed in the circumferential outer wall of the rotor 5; the gas reactant feeding pipe 3 is arranged inside the rotor 5; the edge of the outer wall of the rotor 5 is provided with a first impeller 6, a packing layer 7 and a second impeller 8 in sequence towards the outer side. A gap for the liquid reactant feed pipe 2 to pass through is arranged between the inner wall of the packing layer 7 and the outer wall of the first impeller 6. The bottom of the outer shell 1 is provided with a driving device for driving the stirrer 4 to rotate.
Preferably, but not limited to, the number of the liquid reactant feeding pipes 2 is multiple, the multiple liquid reactant feeding pipes 2 are uniformly arranged in a gap between the inner wall of the packing layer 7 and the outer wall of the first impeller 6 at intervals in the circumferential direction, the bottom of each liquid reactant feeding pipe 2 is of a sealing structure, a liquid outlet 201 is arranged on the outer wall of each liquid reactant feeding pipe 2, the direction of the liquid outlet 201 is the tangential direction of the liquid reactant feeding pipe 2, and the length direction of the outlet is the same as the length direction of the liquid reactant feeding pipe 2. The direction of the liquid outlet 201 is the tangential direction of the liquid reactant feeding pipe 2, so that a narrow pipe effect is generated when the liquid flows out from the liquid reactant feeding pipe 2, the initial speed of liquid flowing out is increased, an ultrathin gas-liquid film is easier to form, the reaction between the liquid and the gas is quickened, and the reaction efficiency is improved.
Preferably, but not limited to, the bottom of the gas reactant feeding pipe 3 is a sealing structure, and a plurality of gas outlet holes 301 are uniformly arranged on the outer wall of the gas reactant feeding pipe 3 at intervals, and the direction of each gas outlet hole 301 is the tangential direction of the gas reactant feeding pipe 3. The gas flows out of the gas outlet holes 301, the initial velocity of the gas is high due to the throat effect, and the gas is accelerated again when passing through the first impeller 6, so that a limit gas film is formed by rapid flow on the convex surface points of the first blades 601.
In order to ensure the sealing performance of the outer casing 1 and to avoid leakage of the product from the inside of the outer casing 1, a dynamic seal bearing 13 is provided at the joint of the stirring shaft 401 and the outer casing 1.
The first impeller 6 comprises a plurality of first blades 601 which have a C-shaped cross section and are uniformly distributed along the circumferential outer wall of the rotor 5 at annular intervals; one end of each first blade 601 is fixedly connected with the outer wall of the rotor 5, and the length direction of each first blade 601 is in the same direction as the length direction of the rotor 5;
the packing layer 7 is of a porous hollow cylindrical structure, the second impeller 8 is sleeved on the circumferential outer wall of the packing layer 7, the second impeller 8 comprises a plurality of second blades 801 with cross sections in an S-shaped structure and uniformly distributed along the circumferential outer wall of the packing layer 7 at annular intervals, and the length direction of the second blades 801 is the same as the length direction of the rotor 5;
the axis of the rotor 5, the axis of the first impeller 6, the axis of the packing layer 7 and the axis of the second impeller 8 are all coincident.
In order to realize synchronous rotation of the rotor 5, the top of the first impeller 6, the top of the packing layer 7 and the second impeller 8, the stirrer 4 further comprises a mounting plate 12, wherein the rotor 5, the top of the first impeller 6, the top of the packing layer 7 and the top of the second impeller 8 are fixedly connected with the lower end face of the mounting plate 12, and a plurality of notches for the gas reactant feeding pipe 3 to pass through the mounting plate 12 to be positioned in the rotor 5 and for the liquid reactant feeding pipe 2 to pass through the mounting plate 12 to be positioned in the gap are arranged on the mounting plate 12.
The stirrer 4 further comprises a stirring shaft 401, one end of the stirring shaft 401 penetrates through the outer shell 1 and is fixedly connected with the inner wall of the rotor 5, and the other end of the stirring shaft is located outside the outer shell 1 and is connected with the driving device.
The basic principle of the scheme is as follows: the driving device realizes centrifugal rotation of the stirrer 4, meanwhile, a gas reactant enters the rotor 5 through the gas reactant feeding pipe 3, and a liquid reactant enters a gap between the inner wall of the packing layer 7 and the outer wall of the first impeller 6 through the liquid reactant feeding pipe 2; under the action of high-speed centrifugation and gas pressure, gas flows from the interior of the rotor 5 to the first guide vane wheel 6, the packing layer 7 and the second guide vane wheel 8 in sequence, and when passing through the first guide vane wheel 6 and the second guide vane wheel 8, the gas is accelerated to pass through, and because of the arrangement of the shape of the blades in the two guide vane wheels, the gas rapidly flows on the convex surface points of the two guide vane wheels to form a limit gas film; under the action of high-speed centrifugation and liquid pressure, the liquid flows through the packing layer 7 and the second impeller 8, and forms an ultrathin gas-liquid film after contacting with a limiting gas film; in the process, the liquid and the gas are dispersed and crushed by the first impeller 6, the packing layer 7 and the second impeller 8 to form a large surface area which is continuously updated, and the tortuous flow passage exacerbates the ultrathin liquid and the surface updating. Thus, the extremely good mass transfer and reaction conditions are formed inside the stirrer 4, because the air inflow and the liquid inflow are automatically controlled by the air and the liquid, an ultrathin air-liquid film is formed, meanwhile, after the ultrathin air-liquid film passes through the second guide impeller 8, an ultrathin air-liquid film is uniformly formed on the convex and concave surfaces, so that the ultrathin air-liquid film forms a reaction between films, and no substance participates in the reaction outside the air-liquid film because of no mass transfer conditions, thereby the reaction is instantaneously completed between films. Meanwhile, the speed between mass transfer objects can be controlled between 7 m/s-12 m/s after the gas-liquid phase passes through the first impeller 6 and the second impeller 8, and vortex-like fluid is formed by the concave surfaces of the first blade 601 and the second blade 801, so that fine grain products are thrown out by the second blade 801, coarse grain products move downwards from the vortex center inside the rotor 5, the non-blocking state is achieved, and the particle size of the reaction products is also controlled. The whole reaction kettle is not easy to be blocked by reactants, the condition that the reaction kettle cannot run for a long time is avoided, the reaction kettle can run for a long time, the overhaul time is shortened, the production efficiency is improved, and the production cost is reduced.
In order to ensure that the temperature in the outer shell 1 is constant and the reaction temperature condition of the product is met, a cooling device is further arranged in the outer shell 1, the cooling device comprises a cooling pipe 9 with a spiral structure, and a cooling liquid inlet 10 and a cooling liquid outlet 11 which are respectively arranged at two sides of the outer shell 1, and the cooling liquid inlet 10 and the cooling liquid outlet 11 are respectively communicated with two ends of the cooling pipe 9; the stirrer 4 is disposed in the cooling tube 9.
As a specific embodiment of the driving device, the driving device comprises a variable frequency motor 14, and a driving belt pulley 15 is arranged on an output shaft of the variable frequency motor 14; the end of the stirring shaft 401 outside the outer housing 1 is provided with a driven pulley 16, and the driving pulley 15 rotates the driven pulley 16 via a belt. The rotation speed of the variable frequency motor 14 is adjustable within the range of 0-1000 rpm, so that the speed between mass transfer objects can be controlled within 7-12 m/s after the gas-liquid phase passes through the first guide impeller 6 and the second guide impeller 8, and the particle size of a reaction product is also controlled.
The bottom side wall of the outer shell 1 is provided with a product discharge port 17 communicated with the inside of the outer shell, the top of the outer shell 1 is provided with a sealing cover 18, and the product discharge port 17 is convenient to take out the product in the outer shell 1.

Claims (7)

1. The reactor comprises an outer shell, a liquid reactant feeding pipe and a gas reactant feeding pipe, and is characterized in that a stirrer is arranged in the outer shell and comprises a rotor with a hollow cylindrical structure, and a plurality of through holes are formed in the outer wall of the circumference of the rotor; the gas reactant feeding pipe is arranged in the rotor;
the edge of the outer wall of the rotor is provided with a first guide impeller, a packing layer and a second guide impeller in sequence outwards; the first impeller comprises a plurality of first blades with a C-shaped cross section and uniformly arranged at intervals along the circumferential outer wall of the rotor in the circumferential direction; one end of each first blade is fixedly connected with the outer wall of the rotor, and the length direction of each first blade is in the same direction as the length direction of the rotor;
the packing layer is of a porous hollow cylindrical structure, and a gap for the liquid reactant feeding pipe to pass through is arranged between the inner wall of the packing layer and the outer wall of the first guide vane wheel;
the second impeller is sleeved on the circumferential outer wall of the packing layer and comprises a plurality of second blades with the cross section of an S-shaped structure and uniformly distributed along the circumferential outer wall of the packing layer at annular intervals, and the length direction of the second blades is in the same direction as the length direction of the rotor;
the axis of the rotor, the axis of the first impeller, the axis of the packing layer and the axis of the second impeller are all coincident; the liquid reactant feeding pipes are circumferentially and uniformly arranged in gaps between the inner wall of the packing layer and the outer wall of the first guide impeller, the bottom of each liquid reactant feeding pipe is of a sealing structure, the outer wall of each liquid reactant feeding pipe is provided with a liquid outlet, the direction of the liquid outlet is the tangential direction of the liquid reactant feeding pipe, and the length direction of the outlet is the same as the length direction of the liquid reactant feeding pipe;
the bottom of the gas reactant feeding pipe is of a sealing structure, a plurality of air outlet holes are uniformly formed in the outer wall of the gas reactant feeding pipe at intervals, and the direction of each air outlet hole is the tangential direction of the gas reactant feeding pipe; the stirring device also comprises a driving device for driving the stirrer to rotate;
after passing through the second guide vane wheel, the ultrathin gas-liquid film is formed on the convex and concave surfaces to form reaction between the films, and no matter participates in the reaction because no mass transfer condition exists outside the gas-liquid film, so that the reaction is completed instantaneously between the films.
2. The reactor according to claim 1, wherein the outer shell is further provided with a cooling device, the cooling device comprises a cooling pipe with a spiral structure, and a cooling liquid inlet and a cooling liquid outlet which are respectively arranged at two sides of the outer shell, and the cooling liquid inlet and the cooling liquid outlet are respectively communicated with two ends of the cooling pipe; the stirrer is arranged in the cooling pipe.
3. The hypergravity membrane-to-membrane reaction kettle according to claim 1, wherein the stirrer further comprises a mounting plate, wherein the rotor, the top of the first impeller, the top of the packing layer and the top of the second impeller are fixedly connected with the lower end face of the mounting plate, and a plurality of notches for allowing the gas reactant feed pipe to pass through the mounting plate and be located in the rotor and for allowing the liquid reactant feed pipe to pass through the mounting plate and be located in the gap are formed in the mounting plate.
4. The hypergravity membrane-to-membrane reaction kettle according to claim 3, wherein the stirrer further comprises a stirring shaft, one end of the stirring shaft penetrates through the outer shell and is fixedly connected with the inner wall of the rotor, and the other end of the stirring shaft is positioned outside the outer shell and is connected with the driving device.
5. The hypergravity membrane-to-membrane reaction kettle according to claim 4, wherein a dynamic seal bearing is arranged at the joint of the stirring shaft and the outer shell.
6. The hypergravity membrane-to-membrane reaction kettle according to claim 4, wherein the driving device comprises a variable frequency motor, and a driving belt pulley is arranged on an output shaft of the variable frequency motor; the end part of the stirring shaft positioned outside the outer shell is provided with a driven belt pulley, and the driving belt pulley drives the driven belt pulley to rotate through a belt.
7. The reactor for hypergravity membrane separation according to claim 3, wherein the side wall of the bottom of the outer shell is provided with a product outlet communicated with the inside of the outer shell, and the top of the outer shell is provided with a sealing cover.
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