CN113877513A - Hypergravity membrane reactor - Google Patents
Hypergravity membrane reactor Download PDFInfo
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- CN113877513A CN113877513A CN202111354111.9A CN202111354111A CN113877513A CN 113877513 A CN113877513 A CN 113877513A CN 202111354111 A CN202111354111 A CN 202111354111A CN 113877513 A CN113877513 A CN 113877513A
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- 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
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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
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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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
- B01J19/0053—Details of the reactor
- B01J19/0073—Sealings
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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
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
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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
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/008—Feed or outlet control devices
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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
- 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
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
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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
- 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
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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
- 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
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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
- 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
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- 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
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- Y02W10/10—Biological treatment of water, waste water, or sewage
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Abstract
The invention discloses a supergravity inter-membrane reaction kettle 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 in 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 inside the rotor; the edge of the outer wall of the rotor is provided with a first guide vane wheel, a packing layer and a second guide vane wheel in sequence towards the outside; the outer shell is provided with a driving device for driving the stirrer to rotate, liquid and gas in the reaction kettle are dispersed and crushed by the first guide vane wheel, the packing layer and the second guide vane wheel to form a large and constantly updated surface area, the zigzag flow channel aggravates the updating of the liquid extreme thin and the surface to form an ultra-thin gas-liquid film, and meanwhile, the ultra-thin gas-liquid film passes through the second guide vane wheel and then forms an ultra-thin gas-liquid phase film on the convex-concave surface, so that the ultra-thin gas-liquid phase film can form a reaction between the films.
Description
Technical Field
The invention relates to the technical field of hypergravity engineering, in particular to a hypergravity inter-membrane reaction kettle.
Background
The basic principle of the supergravity engineering technology is to utilize the unique flow behavior of a multi-phase flow system under the supergravity condition to strengthen the relative speed and mutual contact between phases, thereby realizing the efficient mass and heat transfer process and the efficient chemical reaction process. The mode of acquiring the hypergravity is mainly to form a centrifugal force field by rotating the whole or parts of equipment, and the related multiphase flow system mainly comprises a gas-solid system and a gas-liquid system. Centrifugal force fields (supergravity fields) have been used for phase-to-phase separation for a long time both in daily life and in industrial applications.
The easy reactant that fills in reation kettle among the prior art blocks up, causes and can not run for a long time, has increased maintenance time, leads to reation kettle's production efficiency to reduce, also needs extra manpower and materials to keep equipment normal operating, causes manufacturing cost to improve.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a supergravity inter-membrane reaction kettle, which solves the problems that a filler bed in the existing reaction kettle is easily blocked by reactants, so that the production efficiency is reduced and the production cost is increased.
In order to achieve the purpose of the invention, the technical scheme adopted by the invention is as follows:
the supergravity inter-membrane reaction kettle comprises an outer shell, a liquid reactant feeding pipe and a gas reactant feeding pipe; a stirrer is arranged in the outer shell and comprises a rotor in 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 inside the rotor; the edge of the outer wall of the rotor is provided with a first guide vane wheel, a packing layer and a second guide vane wheel in sequence towards the outside; the first guide impeller comprises a plurality of first blades which have C-shaped cross sections and are uniformly arranged along the circumferential outer wall of the rotor at intervals; 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 the same 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 impeller;
the second guide impeller is sleeved on the circumferential outer wall of the packing layer and comprises a plurality of second blades with cross sections in an S-shaped structure and uniformly arranged along the circumferential outer wall of the packing layer at annular intervals, and the length direction of the second blades is the same as that of the rotor;
the axis of the rotor, the axis of the first guide vane wheel, the axis of the packing layer and the axis of the second guide vane wheel are all overlapped; the stirrer also comprises a driving device for driving the stirrer to rotate.
The basic principle of the scheme is as follows: the driving device realizes the centrifugal rotation of the stirrer, meanwhile, 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 to the first guide vane wheel, the packing layer and the second guide vane wheel from the inside of the rotor in sequence, and when passing through the first guide vane wheel and the second guide vane wheel, the gas passes through the first guide vane wheel and the second guide vane wheel in an accelerated manner, and because of the arrangement of the shapes of the vanes in the two guide vane wheels, the gas rapidly flows on convex points of the two guide vane wheels to form a limit gas film; under the action of high-speed centrifugation and liquid pressure, liquid flows through the packing layer and the second guide impeller and contacts with the limit gas film to form an ultrathin gas-liquid film; in the process, the liquid and the gas are dispersed and crushed by the first guide vane wheel, the filling layer and the second guide vane wheel to form a large and constantly updated surface area, and the zigzag flow channel aggravates the extreme thinness and the updating of the surface of the liquid. Therefore, excellent mass transfer and reaction conditions are formed in the stirrer, the gas and liquid automatically control the gas inflow and the liquid inflow to form an ultrathin gas-liquid film, the ultrathin gas-liquid film passes through the second guide impeller and forms an ultrathin gas-liquid film on the convex-concave surface to form a reaction between the films, and no mass transfer condition exists outside the gas-liquid film, so that no mass participates in the reaction, and the reaction is instantly finished between the films. Meanwhile, the speed between mass transfer objects generated after the gas-liquid phase passes through the first guide impeller and the second guide impeller can be controlled between 7 m/s-12 m/s, and simultaneously, the concave surfaces of the first blade and the second blade form vortex-shaped fluid, so that a fine particle product is thrown out by the second blade, and a coarse particle product moves downwards from the vortex center in the rotor, thereby achieving a non-blocking state and controlling the particle diameter of a reaction product. 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 mode of setting up of liquid reactant inlet pipe, the quantity of liquid reactant inlet pipe is many, many liquid reactant inlet pipes hoop interval evenly set up in the clearance between the inner wall of packing layer and the outer wall of first water conservancy diversion impeller, the bottom of every liquid reactant inlet pipe is seal structure, all be provided with a liquid outlet on the outer wall of every liquid reactant inlet pipe, the direction of liquid outlet is the tangential direction of liquid reactant inlet pipe, the length direction of export and the length direction syntropy of liquid reactant inlet pipe. The direction of liquid export is the tangential direction of liquid reactant inlet pipe for liquid produces the narrow tube effect when flowing out from liquid reactant inlet pipe, increases the initial speed that liquid flows out, makes to form ultra-thin gas-liquid membrane more easily, accelerates liquid and gaseous form the reaction between the membrane, improves reaction efficiency.
Further, as a concrete 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 outlets are uniformly arranged on the outer wall of the gas reactant feeding pipe at intervals, and the direction of each air outlet 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 tube effect, and the gas is accelerated again when passing through the first guide vane wheel, so that the gas flows rapidly on the convex point of the first blade to form a limit gas film.
Furthermore, in order to keep the temperature in the outer shell constant and ensure that the reaction temperature condition of the product is met, a cooling device is also arranged in the outer shell, the cooling device comprises a cooling pipe in 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 the synchronous rotation of rotor, first water conservancy diversion impeller top, packing layer top and second water conservancy diversion impeller, the agitator still includes the mounting panel, and rotor, first water conservancy diversion impeller top, packing layer top and second water conservancy diversion impeller top all with the lower terminal surface fixed connection of mounting panel, be provided with a plurality ofly on the mounting panel and be used for the gaseous reactant inlet pipe to pass the mounting panel and be located the rotor inside and be used for the liquid reactant inlet pipe to pass the breach that the mounting panel is located the clearance.
Furthermore, the stirrer also 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 and avoid the leakage of products from the inner part of the outer shell, a dynamic sealing bearing is arranged at the joint of the stirring shaft and the outer shell.
Further, as a specific implementation manner of the driving device, the driving device comprises a variable frequency motor, and an output shaft of the variable frequency motor is provided with a driving belt pulley; 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.
Furthermore, a product discharge port communicated with the inside of the outer shell is formed in the side wall of the bottom of the outer shell, a sealing cover is arranged at the top of the outer shell, and the product in the outer shell can be conveniently taken out through the product discharge port.
The invention has the beneficial effects that: 1. the liquid and gas in the reaction kettle are dispersed and crushed by the first guide vane wheel, the packing layer and the second guide vane wheel to form a large and constantly updated surface area, the zigzag flow channel aggravates the updating of the liquid extreme and the surface to form an ultra-thin gas-liquid film, and the ultra-thin gas-liquid film passes through the second guide vane wheel and then forms the ultra-thin gas-liquid film on the convex-concave surface to form a reaction between the films.
2. The driving device of the scheme can drive the stirrer to rotate centrifugally at different speeds, and meanwhile, the concave surfaces of the first blade and the second blade form vortex-shaped fluid, so that fine particle products are thrown out by the second blade, and coarse particle products move downwards from the vortex center inside the rotor, so that a non-blocking state is achieved, and the particle diameter 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 supergravity inter-membrane reactor.
FIG. 2 is an enlarged schematic view of a liquid reactant feed tube.
FIG. 3 is an enlarged schematic view of a gaseous reactant feed tube.
FIG. 4 is a schematic cross-sectional view of the stirrer.
Fig. 5 is a schematic perspective view of the stirrer.
Wherein, 1, an outer shell; 2. a liquid reactant feed; 201. a liquid outlet; 3. a gaseous reactant feed; 301. an air outlet; 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 coolant inlet; 11. a coolant outlet; 12. mounting a plate; 13. a dynamic seal bearing; 14. a variable frequency motor; 15. a drive pulley; 16. a driven pulley; 17. a product discharge port; 18. and (7) sealing the cover.
Detailed Description
The following description of the embodiments of the present invention is provided to facilitate the 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 it will be apparent to those skilled in the art that various changes may be made without departing from the spirit and scope of the invention as defined and defined in the appended claims, and all matters produced by the invention using the inventive concept are protected.
As shown in fig. 1 to 5, the present invention provides a supergravity inter-membrane reactor, which comprises an outer shell 1, a liquid reactant feeding pipe 2 and a gas reactant feeding pipe 3. A stirrer 4 is arranged in the outer shell 1, the stirrer 4 comprises a rotor 5 in a hollow cylindrical structure, and a plurality of through holes are formed in the circumferential outer wall of the rotor 5; the gaseous reactant feed conduit 3 is arranged inside the rotor 5; the edge of the outer wall of the rotor 5 is provided with a first guide vane wheel 6, a packing layer 7 and a second guide vane wheel 8 in sequence towards the outside. A gap for the liquid reactant feeding pipe 2 to pass through is arranged between the inner wall of the packing layer 7 and the outer wall of the first guide vane wheel 6. The bottom of the outer shell 1 is provided with a driving device for driving the stirrer 4 to rotate.
Preferably, but not limitingly, the number of liquid reactant inlet pipes 2 is many, many liquid reactant inlet pipes 2 are circumferentially arranged in the gap between the inner wall of packing layer 7 and the outer wall of first guide vane wheel 6 at intervals, the bottom of each liquid reactant inlet pipe 2 is a sealing structure, a liquid outlet 201 is arranged on the outer wall of each liquid reactant inlet pipe 2, the direction of liquid outlet 201 is the tangential direction of liquid reactant inlet pipe 2, and the length direction of the outlet is the same as the length direction of liquid reactant inlet pipe 2. The direction of liquid export 201 is the tangential direction of liquid reactant inlet pipe 2 for liquid produces the throat effect when flowing out from liquid reactant inlet pipe 2, increases the initial speed that liquid flows out, makes to form ultra-thin gas-liquid membrane more easily, accelerates liquid and gas formation reaction between the membrane, improves reaction efficiency.
Preferably, but not limitatively, the bottom of the gas reactant feeding pipe 3 is a sealed structure, a plurality of gas outlets 301 are uniformly arranged on the outer wall of the gas reactant feeding pipe 3 at intervals, and the direction of each gas outlet 301 is the tangential direction of the gas reactant feeding pipe 3. The gas flows out from the gas outlet hole 301, the initial velocity of the gas is high due to the narrow tube effect, and the gas is accelerated again when passing through the first guide vane wheel 6, so that the gas rapidly flows on the convex point of the first blade 601 to form a limit gas film.
In order to ensure the sealing performance of the outer shell 1 and avoid the leakage of the product from the inside of the outer shell 1, a dynamic seal bearing 13 is arranged at the joint of the stirring shaft 401 and the outer shell 1.
The first guide impeller comprises a plurality of first blades 601 which have C-shaped cross sections and are uniformly arranged along the circumferential outer wall of the rotor 5 at intervals; one end of each first blade 601 is fixedly connected with the outer wall of the rotor 5, and the length direction of the first blade 601 is the same as that of the rotor 5;
the packing layer 7 is a porous hollow cylindrical structure, the second guide vane wheel 8 is sleeved on the circumferential outer wall of the packing layer 7, the second guide vane wheel 8 comprises a plurality of second vanes 801 with cross sections in an S-shaped structure and uniformly arranged at intervals along the circumferential outer wall of the packing layer 7 in an annular manner, and the length direction of each second vane 801 is the same as the length direction of the rotor 5;
the axial line of the rotor 5, the axial line of the first guide vane wheel 6, the axial line of the packing layer 7 and the axial line of the second guide vane wheel 8 are all coincided.
In order to realize the synchronous rotation of rotor 5, first guide vane wheel 6 top, packing layer 7 top and second guide vane wheel 8, agitator 4 still includes mounting panel 12, rotor 5, first guide vane wheel 6 top, packing layer 7 top and second guide vane wheel 8 top all with mounting panel 12's lower terminal surface fixed connection, be provided with a plurality ofly on the mounting panel 12 and be used for supplying gaseous reactant inlet pipe 3 to pass mounting panel 12 and be located rotor 5 inside and be used for supplying liquid reactant inlet pipe 2 to pass the breach that mounting panel 12 is located the clearance.
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 401 is located outside the outer shell 1 and is connected with a driving device.
The basic principle of the scheme is as follows: the driving device realizes the centrifugal rotation of the stirrer 4, simultaneously, 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 guide vane wheel 6 through the liquid reactant feeding pipe 2; under the action of high-speed centrifugation and gas pressure, gas flows to the first guide vane wheel 6, the packing layer 7 and the second guide vane wheel 8 from the inside of the rotor 5 in sequence, and passes through the first guide vane wheel 6 and the second guide vane wheel 8 at an accelerated speed, and because of the arrangement of the shape of the blades in the two guide vane wheels, the gas rapidly flows on the convex points of the two guide vane wheels to form a limit gas film; under the action of high-speed centrifugation and liquid pressure, liquid flows through the packing layer 7 and the second guide impeller 8 and contacts with the limit gas film to form an ultrathin gas-liquid film; in the process, the liquid and the gas are dispersed and crushed by the first guide vane wheel 6, the filler layer 7 and the second guide vane wheel 8 to form a large and constantly updated surface area, and the zigzag flow channel promotes the extreme thinness and the updating of the surface of the liquid. Thus, excellent mass transfer and reaction conditions are formed inside the stirrer 4, the gas and liquid automatically control the gas inflow and the liquid inflow, so that an ultrathin gas-liquid film is formed, meanwhile, the ultrathin gas-liquid film forms ultrathin gas-liquid phase films on the convex-concave surface after passing through the second guide impeller 8, so that the ultrathin gas-liquid phase films are formed to react among the films, and no mass transfer condition exists outside the gas-liquid film, so that no mass participates in the reaction, and the reaction is instantly finished among the films. Meanwhile, the speed between mass transfer objects generated after the gas-liquid phase passes through the first guide impeller 6 and the second guide impeller 8 can be controlled between 7 m/s-12 m/s, and simultaneously, the concave surfaces of the first blade 601 and the second blade 801 form vortex-shaped fluid, so that a fine particle product is thrown out by the second blade 801, and a coarse particle product moves downwards from the vortex center in the rotor 5, thereby achieving a non-blocking state and controlling the particle size of a reaction product. 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 keep the temperature in the outer shell 1 constant and ensure that the reaction temperature condition of the product is met, a cooling device is also arranged in the outer shell 1, the cooling device comprises a cooling pipe 9 in 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 inside the cooling pipe 9.
As a specific embodiment of the driving device, the driving device includes a variable frequency motor 14, and a driving pulley 15 is disposed on an output shaft of the variable frequency motor 14; the end of the stirring shaft 401 outside the outer shell 1 is provided with a driven pulley 16, and the driving pulley 15 drives the driven pulley 16 to rotate through a belt. The rotating speed of the variable frequency motor 14 is adjustable within the range of 0-1000 r/min, so that the speed of mass transfer objects generated after gas-liquid communication passes through the first guide impeller 6 and the second guide impeller 8 can be controlled within the range of 7-12 m/s, and the particle size of reaction products can be controlled.
A product discharge port 17 communicated with the inside of the outer shell 1 is formed in the side wall of the bottom of the outer shell 1, a sealing cover 18 is arranged at the top of the outer shell 1, and the product in the outer shell 1 can be conveniently taken out through the product discharge port 17.
Claims (9)
1. A supergravity inter-membrane reaction kettle 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 in a hollow cylindrical structure, and a plurality of through holes are formed in the circumferential outer wall of the rotor; the gas reactant feed pipe is arranged inside the rotor;
the edge of the outer wall of the rotor is provided with a first guide vane wheel, a packing layer and a second guide vane wheel in sequence towards the outside; the first guide impeller comprises a plurality of first blades which are of C-shaped cross sections and are uniformly arranged along the circumferential outer wall of the rotor at intervals; 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 the same 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 formed between the inner wall of the packing layer and the outer wall of the first guide impeller;
the second guide impeller is sleeved on the circumferential outer wall of the packing layer and comprises a plurality of second blades with cross sections in an S-shaped structure and uniformly arranged along the circumferential outer wall of the packing layer at annular intervals, and the length direction of the second blades is the same as that of the rotor;
the axis of the rotor, the axis of the first guide vane wheel, the axis of the packing layer and the axis of the second guide vane wheel are all overlapped;
the stirrer also comprises a driving device for driving the stirrer to rotate.
2. The ultra-gravity inter-membrane reaction kettle according to claim 1, wherein the number of the liquid reactant feeding pipes is multiple, the multiple liquid reactant feeding pipes are circumferentially and uniformly arranged in a gap between the inner wall of the packing layer and the outer wall of the first guide impeller at intervals, the bottom of each liquid reactant feeding pipe is a sealing structure, a liquid outlet is formed in the outer wall of each liquid reactant feeding pipe, the direction of the liquid outlet is the tangential direction of the liquid reactant feeding pipes, and the length direction of the outlet is the same as the length direction of the liquid reactant feeding pipes.
3. The high-gravity inter-membrane reaction kettle according to claim 2, wherein the bottom of the gas reactant feeding pipe is provided with a sealing structure, a plurality of gas outlets are uniformly arranged on the outer wall of the gas reactant feeding pipe at intervals, and the direction of each gas outlet is the tangential direction of the gas reactant feeding pipe.
4. The high-gravity inter-membrane reaction kettle according to claim 1, wherein a cooling device is further arranged in the outer shell, the cooling device comprises a cooling pipe in 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.
5. The high-gravity inter-membrane reaction kettle according to claim 1, wherein the stirrer further comprises a mounting plate, the rotor, the top of the first guide vane wheel, the top of the packing layer and the top of the second guide vane wheel are fixedly connected with the lower end surface of the mounting plate, and a plurality of notches are arranged on the mounting plate, through which the gas reactant feeding pipe passes and is positioned inside the rotor, and through which the liquid reactant feeding pipe passes and is positioned in the gap.
6. The high-gravity inter-membrane reaction kettle according to claim 5, 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 a driving device.
7. The high-gravity inter-membrane reaction kettle according to claim 6, wherein a dynamic seal bearing is arranged at the joint of the stirring shaft and the outer shell.
8. The high-gravity membrane reactor according to claim 5, wherein the driving device comprises a variable frequency motor, and a driving pulley is arranged on an output shaft of the variable frequency motor; the end part of the stirring shaft, which is 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.
9. The high-gravity membrane reactor as claimed in claim 5, wherein a product outlet is formed in the side wall of the bottom of the outer shell and communicated with the inside of the outer shell, and a sealing cover is arranged at the top of the outer shell.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111354111.9A CN113877513B (en) | 2021-11-15 | 2021-11-15 | Reaction kettle between hypergravity films |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111354111.9A CN113877513B (en) | 2021-11-15 | 2021-11-15 | Reaction kettle between hypergravity films |
Publications (2)
| Publication Number | Publication Date |
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| CN113877513A true CN113877513A (en) | 2022-01-04 |
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| CN115212829A (en) * | 2022-06-14 | 2022-10-21 | 湖北恒信石化设备有限公司 | High-shear microbubble jet reaction kettle |
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| CN113877513B (en) | 2023-06-27 |
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