CN210159617U - High-flow high-efficiency multiphase reactor - Google Patents
High-flow high-efficiency multiphase reactor Download PDFInfo
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- CN210159617U CN210159617U CN201920840216.7U CN201920840216U CN210159617U CN 210159617 U CN210159617 U CN 210159617U CN 201920840216 U CN201920840216 U CN 201920840216U CN 210159617 U CN210159617 U CN 210159617U
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Abstract
The utility model discloses a large-flow high-efficiency multiphase reactor, which comprises an air/liquid outlet pipe, an air/liquid inlet pipe, an air/liquid pipe, a top cover and a movable plate, the price fixing, the feed liquor pipe, the drain pipe, price fixing upper portion is located to the coaxial interval of driving disk, the bottom of driving disk and the top of price fixing form the mixed reacting chamber in clearance, the quotation of the nearly center pin of driving disk is equipped with the liquid hole of ventilating of a plurality of intercommunication bottoms, driving disk upper portion is equipped with inclosed top cap, wind/liquid pipe passes the bottom of top cap and ventilates/liquid hole intercommunication, give vent to anger/liquid pipe, it locates top cap top or lateral part to admit air/liquid pipe branch, the quotation of the nearly center pin of price fixing is equipped with the feed liquor hole of a plurality of intercommunication top surfaces and communicates with the feed liquor pipe, the drain pipe is located the bottom of price fixing and is communicated with the guiding gutter that the outer fringe side of price fixing. The utility model has the characteristics of handling capacity is big, mass transfer and heat transfer rate are high, can be used to double-phase and heterogeneous mixture, steerable reaction condition.
Description
Technical Field
The utility model belongs to the technical field of chemical industry equipment, concretely relates to large-traffic high-efficient heterogeneous reactor that handling capacity is big, mass transfer and heat transfer rate are high, can be used to double-phase and heterogeneous, steerable reaction condition.
Background
In the fields of metallurgy, chemistry, chemical industry, petrifaction, medicine, food and the like, most of chemical reactions relate to gas-liquid or liquid-liquid multiphase mixed mass transfer, particularly the treatment of waste gas and waste water in industries such as various large steel plants, nonferrous metal smelting plants, thermal power plants, chemical plants and the like, and the large-output treatment is difficult to cause that many industries can not reach the national emission standard. A need exists for an apparatus that has a high throughput, high efficiency, and low energy consumption. During a chemical reaction, the rate of the chemical reaction can only be increased by increasing the rate of heat and mass transfer between the reactants.
The traditional chemical reaction equipment comprises a packed tower, a plate tower, a spray tower, a fixed bed, a reaction kettle and the like, but has the following problems: 1. the two-phase contact time is short, the mass transfer distance is long, and the reaction balance is difficult to achieve; 2. insufficient renewal of the two-phase contact surface; 3. the equipment is huge, the investment is large and the operation cost is high.
In the prior art, the filler is rotated at a high speed by a supergravity device and a rotating packed bed device to cut liquid drops or bubbles to form liquid filaments and a liquid film, so that the purposes of increasing the contact area of two phases and continuously updating the interfaces of the two phases are achieved, and the mass transfer effect can be enhanced. However, the supergravity equipment and the rotary packed bed equipment have the problems of short two-phase contact time and high rotating speed, which causes high energy consumption.
Certainly, in order to solve the defects of the mass transfer process, the utility model also researches two single or multiple fax discs or reaction devices of CN106111047 and CN106111037, although the mixing lightness and the mass transfer efficiency are effectively improved, the liquid inlet of the mass transfer disc is close to the shaft, which causes small space, less liquid inlet and air inlet holes and difficult expansion of the treatment capacity; in addition, the mass transfer tray is small due to structural limitation, and the contact time is shortened after the processing amount is increased.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a large-traffic high-efficient heterogeneous reactor that handling capacity is big, mass transfer and heat transfer rate are high, can be used to double-phase and heterogeneous, steerable reaction condition.
The purpose of the utility model is realized like this: comprises an air/liquid outlet pipe, an air/liquid inlet pipe, an air/liquid pipe, a top cover, a movable plate, a fixed plate, a liquid inlet pipe and a liquid outlet pipe, the movable disc is coaxially arranged at the upper part of the fixed disc at intervals, a gap mixing reaction chamber is formed between the bottom of the movable disc and the top of the fixed disc, the disc surface of the movable disc near the central shaft is provided with a plurality of air/liquid holes communicated with the bottom, the upper part of the movable disc is provided with a closed top cover, the wind/liquid pipe passes through the bottom of the top cover and is communicated with the ventilation/liquid hole, the gas/liquid outlet pipe and the gas/liquid inlet pipe are respectively arranged at the top or the side part of the top cover, the disc surface of the fixed disc near the central shaft is provided with a plurality of liquid inlet holes communicated with the top surface and communicated with a liquid inlet pipe, the drain pipe is arranged at the bottom of the fixed disc and is communicated with a diversion trench formed on the outer edge side of the fixed disc, and the movable disc is connected with the driving end of the driving device through a central shaft.
The utility model has the advantages that:
1. the utility model discloses utilize the shearing that the high-speed rotation of pivoted driving disk and fixed price fixed plate produced relatively, the crushing effect, liquid phase and/or solid phase that will get into mixed reaction chamber cut into micron order physical dimension's droplet, thereby high efficiency enlarges the specific surface area that makes two contact, and the motion trail of double-phase droplet between two dishes is the spiral form removal of gradually opening by the inboard outside of annular, not only can strengthen double-phase or heterogeneous droplet and mix and the surface renewal, and make the material stream in the mixed reaction chamber can take place to beat at wherein and revolve the formation torrent through the relative motion between two dishes, the reaction time of contact between the material has been prolonged, thereby mass transfer and heat transfer rate have been improved greatly, reaction rate has been strengthened.
2. The utility model can be provided with one or more liquid inlet pipes and corresponding liquid inlet holes as required, thereby not only treating gas-liquid or liquid-liquid two phases, but also treating gas-liquid, gas-liquid-solid or liquid-solid multiple phases, and having the advantage of wide application field.
3. The utility model discloses can get into the flow of mixing the reacting chamber, the rotational speed of driving disk, the interval between driving disk and the fixed plate through adjusting each item material according to the chemical reaction condition of difference to the mixing intensity, mixing time, the reaction temperature of steerable reactant, thereby have stronger adaptability.
4. The utility model discloses the resultant liquid phase after the hybrid reaction is involute spiral threadiness through the high-speed rotation of driving disk and removes the edge of deciding the dish, flows down from deciding the dish outer fringe along with gravity and gets into the guiding gutter and flow out from the drain pipe nature, and the gas phase gives vent to anger/the liquid pipe nature of driven plate top discharges to need not extra power, consequently whole energy consumption is lower.
5. The utility model discloses can be according to the handling capacity, through the passageway quantity that increases the feed liquor hole and the outage in the interior ventilation/liquid hole of driving disk, the price fixing, the mixed reacting chamber distance between adjustment driving disk and the price fixing and the rotational speed of driving disk to and enlarge the diameter of driving disk and price fixing, all can effectively improve the handling capacity, the adaptation elasticity of handling capacity is higher.
Drawings
FIG. 1 is a schematic view of the structure of the present invention;
FIG. 2 is an isometric view of FIG. 1;
FIG. 3 is a schematic view of the structure of the movable plate and the fixed plate of FIG. 1
FIG. 4 is a schematic view of a three-dimensional cross-sectional structure of the movable plate of FIG. 3 in the plate surface direction;
FIG. 5 is a schematic view of a three-dimensional cutting structure of the movable plate of FIG. 3;
FIG. 6 is a schematic three-dimensional sectional structure of the fixed plate shown in FIG. 3;
in the figure: 1-gas/liquid outlet pipe, 2-gas/liquid inlet pipe, 3-wind/liquid pipe, 4-top cover, 5-movable disc, 501-gas/liquid inlet hole, 502-annular groove, 503-gas phase buffer chamber, 504-rib plate I, 6-fixed disc, 601-liquid inlet hole, 602-flow guide groove, 603-flow guide groove, 604-rib plate II, 7-liquid inlet pipe, 8-liquid outlet pipe, 9-bearing seat, 10-transmission mechanism, 11-motor and 12-frame.
Detailed Description
The present invention is further described with reference to the following drawings and examples, but the present invention is not limited thereto in any way, and any modification or improvement based on the teaching of the present invention is within the protection scope of the present invention.
As shown in fig. 1 to 6, the large flow high efficiency multiphase reactor of the present invention comprises an air/liquid outlet pipe 1, an air/liquid inlet pipe 2, an air/liquid pipe 3, a top cover 4, a movable disk 5, a fixed disk 6, a liquid inlet pipe 7, and a liquid outlet pipe 8, wherein the movable disk 5 is coaxially disposed on the fixed disk 6 at intervals, the bottom of the movable disk 5 and the top of the fixed disk 6 form a gap mixing reaction chamber, the disk surface of the movable disk 5 near the center axis is provided with a plurality of air/liquid holes 501 communicating with the bottom, the upper portion of the movable disk 5 is provided with a sealed top cover 4, the air/liquid pipe 3 passes through the bottom of the top cover 4 to communicate with the air/liquid holes 501, the air/liquid outlet pipe 1 and the air/liquid inlet pipe 2 are respectively disposed on the top or side of the top cover 4, the liquid inlet hole 601 of the fixed disk 6 near the center axis is, the liquid outlet pipe 8 is arranged at the bottom of the fixed disc 6 and is communicated with a flow guide groove 604 formed on the outer edge side of the fixed disc 6, and the movable disc 5 is connected with the driving end of the driving device through a central shaft.
The upper surface of the fixed disc 6 is provided with at least two layers of flow guiding ribs or flow guiding grooves 602 which are uniformly distributed around the central shaft, and the lower surface of the movable disc 5 near the central shaft is provided with a plurality of layers of annular grooves 502.
The depth of the annular groove 502 is 40.5-8.0 mm, the camber angle is 40-80 degrees, and the distance between every two adjacent layers of grooves is 5-30 mm.
The fixed disc 6 is provided with at least one layer of liquid inlet holes 601 which are uniformly distributed in each layer around the central shaft, and the movable disc 5 is provided with at least one layer of ventilation/liquid holes 501 which are uniformly distributed in each layer around the central shaft.
The flow guiding ribs or grooves 602 on the fixed disk 6 are of a straight strip-shaped or parabolic structure, and the straight strip-shaped flow guiding ribs or grooves 602 on the fixed disk 6 are distributed in a straight spoke shape or an inclined spoke shape.
The upper part of the disc surface of the movable disc 5 is provided with a gas phase buffer chamber 503 which is sealed around the central shaft, the air/liquid pipe 3 is communicated with the gas phase buffer chamber 503, and the air/liquid hole 501 is arranged on the disc surface of the movable disc 5 in the gas phase buffer chamber 503.
The disc surface of the movable disc 5 is provided with a plurality of exhaust holes communicated with the air/liquid outlet pipe 1 outside the gas phase buffer chamber 503.
The distance between the mixing reaction chambers between the movable disc 5 and the fixed disc 6 is 0.5-10 mm, and the diameter of the ventilation/liquid hole 501 and/or the liquid inlet hole 601 is 0.2-10 mm.
The fixed disc 6 is uniformly provided with at least two groups of mutually independent liquid inlet holes 601 around the central shaft and communicated with corresponding different liquid inlet pipes 7, and the liquid inlet holes 601 are uniformly distributed at 1/3 positions corresponding to the disc surface diameter of the movable disc 5.
The rotating speed of the movable disc 5 is 50-5000 r/min, and the diameter of the movable disc 5 and/or the fixed disc 6 is 300-10000 mm.
One side of the upper surface of the movable disc 5 close to the edge is provided with a balance adjusting hole, and a balance adjusting block is embedded or screwed in the balance adjusting hole.
The driving device comprises a motor 11 and a driving mechanism 10, wherein a driving shaft of the motor is connected with an input shaft of the driving mechanism 10, and an output shaft of the driving mechanism 10 is connected with a central shaft of the movable disc 5.
The transmission mechanism 10 is a bevel gear transmission mechanism or a turbine worm transmission mechanism.
The utility model discloses the theory of operation:
the utility model discloses utilize the shearing that the high-speed rotation of pivoted driving disk and fixed price dish produced relatively, crushing effect, liquid phase and/or solid phase that will get into the mixed reaction chamber cut into micron order physical dimension's droplet, thereby high-efficient the specific surface area that enlarges and make two contacts, and the motion trail of double-phase droplet between two dishes is by the annular inboard outside to be involute spiral form and move, not only can strengthen double-phase or heterogeneous droplet and mix and surface renewal, and make the material flow in the mixed reaction chamber can take place to beat and revolve among them and form the torrent through the relative motion between two dishes, the reaction time of contact between the material has been prolonged, thereby mass transfer and heat transfer rate have been improved greatly, reaction rate has been strengthened; one or more liquid inlet pipes and corresponding liquid inlet holes can be arranged according to requirements, so that not only can gas-liquid or liquid-liquid two phases be treated, but also gas-liquid, gas-liquid-solid or liquid-solid multiple phases can be treated, and the device has the advantage of wide application field; the mixing intensity, mixing time and reaction temperature of reactants can be controlled by adjusting the flow of each material entering the mixing reaction chamber, the rotating speed of the movable disc and the distance between the movable disc and the fixed disc according to different chemical reaction conditions, so that the reaction device has strong adaptability; the utility model discloses the product liquid phase after the mixing reaction is the edge that the involute spiral line form removed the fixed disk through the high-speed rotation of movable disk, especially gaseous phase mixing reaction, the liquid phase gets into from the feed liquor pipe of fixed disk bottom and the gaseous phase mixing reaction that gets into from the movable disk of upper portion, the fluid that has mixed flows down from the outermost fringe in the clearance between two dishes and gets into the guiding gutter, later gaseous phase is upwards to flow out the reactor naturally from the gas outlet/liquid pipe at top of the driven disk, and the liquid phase then flows out the reactor naturally from guiding gutter and drain pipe along with gravity, thereby realize gas-liquid phase separation, the separator outflow process does not need extra power, therefore whole energy consumption is lower; can be according to the handling capacity, through increasing the passageway quantity of ventilating in the movable disk/liquid hole, the feed liquor hole in the fixed disk and outage, adjust the mixed reaction chamber distance between movable disk and the fixed disk and the rotational speed of movable disk to and enlarge the diameter of movable disk and fixed disk, all can effectively improve the handling capacity, the adaptation elasticity of handling capacity is higher. Furthermore, the upper surface of the fixed disc is provided with at least two layers of flow guiding ribs or flow guiding grooves which are uniformly distributed around the central shaft, and the problem of ineffective flow of short circuit caused by outward sliding of droplets due to the centrifugal force of the movable disc is solved; and the guide groove or the guide rib can be matched with the movable disc to cut the microdroplets into liquid drops with extremely small sizes, so that the specific surface area of the microdroplets is increased rapidly, the mixing strength and the mass transfer rate are further enhanced greatly, and the reaction rate is enhanced. Furthermore, the lower surface of the movable disc is provided with a plurality of layers of annular grooves near the central axis, and sheared and broken micro-droplets can form turbulent flow through the plurality of layers of annular grooves, so that the contact reaction time among all the parts is effectively prolonged. Furthermore, the fixed plate is provided with at least one layer and a plurality of evenly distributed's in every layer feed liquor hole around the center pin, and the movable plate is provided with at least one layer and a plurality of evenly distributed's in every layer ventilation/liquid hole around the center pin, through the material through-hole of multilayer and a plurality of equipartitions, can effectively increase the volume of advancing out of reaction item as required to effectively improve holistic handling capacity. Further, the quotation upper portion of driving disk is provided with around center pin and inclosed gaseous phase surge chamber, can effectively cushion the gas flow fluctuation and the pressure variation in the mixed reaction room of admitting air/liquid pipe through gaseous phase surge chamber to make the reaction of mixed reaction room steady and relax, in order to improve the quality of mixed reaction product. Furthermore, one side of the upper surface of the movable disc close to the edge is provided with a balance adjusting hole, and a balance adjusting block is embedded or screwed, so that the dynamic balance of the movable disc can be effectively adjusted through the balance adjusting block, the stability in the mixed reaction chamber can be improved, and the batch uniformity of the mixed reactants is improved. To sum up, the utility model has the characteristics of handling capacity is big, mass transfer and heat transfer rate are high, can be used to double-phase and heterogeneous, steerable reaction condition.
Example 1
The diameters of the movable disc and the fixed disc are 1.5 m, a dilute alkali solution and oxidant solution system is adopted, a single-stage solution absorption experiment of low-concentration NOx at the rear end of the single-stage solution absorption experiment is carried out,the gas treatment amount reaches 3500 m3At gas-liquid volume ratio as high as 50:1, the research result shows that the NOx (wherein NO is in 457.9 ppm concentration) can be obtained2151.6 ppm, NO 306.3 ppm) to 58.1ppm (wherein NO is252.9 ppm, NO 5.2 ppm). A good effect is obtained. The test result shows that the efficiency of absorbing low-concentration NOx by the NOx absorbing device can reach 87.31%.
Example 2
The diameters of the movable disc and the fixed disc are 2 m, the urea solution is adopted to carry out the absorption experiment of the nitrogen oxides generated in the noble metal dissolving process and the single-stage solution absorption experiment of the low-concentration NOx at the rear end, and the treatment gas amount reaches 9800 m3At gas-liquid volume ratio as high as 30:1, the research result shows that NOx (NO) with concentration of 500.6 ppm can be obtained2142.6 ppm, NO 358.0 ppm) to 50.1 ppm (wherein NO235.0 ppm, NO 15.1 ppm). A good effect is obtained. Test results show that the efficiency of the NOx absorption device for absorbing low-concentration NOx can reach 89.99%.
Example 3
The diameters of the moving disc and the fixed disc are 1.5 m, a dilute alkali solution and oxidant solution system is adopted, a single-stage solution absorption experiment of low-concentration NOx at the rear end of the single-stage solution absorption experiment is carried out, and the treatment gas amount reaches 5600 m3At a gas-liquid volume ratio as high as 40:1, the research result shows that the NOx (wherein NO is contained in the NOx) with the concentration of 481.5 ppm can be obtained2126.4 ppm, NO 355.1 ppm) to 47.8ppm (wherein NO243.4 ppm, NO 4.4 ppm). A good effect is obtained. The test results show that the efficiency of absorbing low-concentration NOx by the NOx absorbing device can reach 90.07%.
Example 4
The diameters of the movable disc and the fixed disc are 2 m, dilute alkali liquor and ozone solution are adopted to carry out a nitrogen oxide absorption experiment generated in a noble metal dissolving process, a single-stage solution absorption experiment of low-concentration NOx at the rear end is carried out, and the treatment gas flow reaches 9800 m3At gas-liquid volume ratio as high as 60:1, the research result shows that the NOx (wherein NO is contained in the NOx) with the concentration of 472.9 ppm can be obtained2143.1ppm, NO 329.8 ppm) to 55.3 ppm (wherein NO240.6 ppm, NO 14.7 ppm). Obtain goodThe effect of (1). The test results show that the efficiency of absorbing low-concentration NOx by the NOx absorbing device can reach 88.31%.
Claims (9)
1. A high-flow high-efficiency multiphase reactor is characterized by comprising an air/liquid outlet pipe (1), an air/liquid inlet pipe (2), an air/liquid pipe (3), a top cover (4), a movable disc (5), a fixed disc (6), a liquid inlet pipe (7) and a liquid outlet pipe (8), wherein the movable disc (5) is coaxially arranged on the upper part of the fixed disc (6) at intervals, a gap mixing reaction chamber is formed between the bottom of the movable disc (5) and the top of the fixed disc (6), a disc surface of the movable disc (5) close to a central shaft is provided with a plurality of ventilation/liquid holes (501) communicated with the bottom, the upper part of the movable disc (5) is provided with a closed top cover (4), the air/liquid pipe (3) penetrates through the bottom of the top cover (4) to be communicated with the ventilation/liquid holes (501), the air/liquid outlet pipe (1) and the air/liquid inlet pipe (2, the liquid inlet pipe (8) is arranged at the bottom of the fixed disc (6) and is communicated with the outer edge side of the fixed disc (6) to form a flow guide groove, and the movable disc (5) is connected with the driving end of the driving device through the central shaft.
2. The high-flow and high-efficiency multiphase reactor according to claim 1, wherein the upper surface of the fixed plate (6) is provided with at least two layers of flow guiding ribs or flow guiding grooves (602) which are uniformly distributed around a central axis, and the lower surface of the movable plate (5) is provided with a plurality of layers of annular grooves (502) near the central axis.
3. The high-flow high-efficiency multiphase reactor according to claim 2, characterized in that the fixed plate (6) is provided with at least one layer and a plurality of evenly distributed liquid inlet holes (601) per layer around the central axis, and the movable plate (5) is provided with at least one layer and a plurality of evenly distributed aeration/liquid holes (501) per layer around the central axis.
4. The high-flow and high-efficiency multiphase reactor according to claim 3, wherein the flow guiding ribs or grooves (602) on the fixed disk (6) are of a straight-bar or parabolic structure, and the straight-bar flow guiding ribs or grooves (602) on the fixed disk (6) are distributed in a straight spoke shape or an inclined spoke shape.
5. The high-flow high-efficiency multiphase reactor according to claim 3, wherein the upper part of the plate surface of the movable plate (5) is provided with a gas phase buffer chamber (503) which is sealed around the central shaft, the air/liquid pipe (3) is communicated with the gas phase buffer chamber (503), and the air/liquid hole (501) is arranged on the plate surface of the movable plate (5) in the gas phase buffer chamber (503).
6. The high-flow high-efficiency multiphase reactor according to claim 3, 4 or 5, wherein the distance between the mixing reaction chambers between the moving plate (5) and the fixed plate (6) is 0.5-10 mm, and the diameter of the aeration/liquid hole (501) and/or the liquid inlet hole (601) is 0.2-10 mm.
7. The high-flow high-efficiency multiphase reactor according to claim 6, wherein the fixed plate (6) is uniformly provided with at least two groups of mutually independent liquid inlet holes (601) around the central shaft and is communicated with corresponding different liquid inlet pipes (7), and the liquid inlet holes (601) are uniformly distributed at 1/3 positions corresponding to the disc surface diameter of the movable plate (5).
8. The high-flow high-efficiency multiphase reactor according to claim 6, wherein the rotating speed of the movable disc (5) is 50-5000 r/min, and the diameter of the movable disc (5) and/or the fixed disc (6) is 300-10000 mm.
9. The high-flow high-efficiency multiphase reactor according to claim 6, wherein a balance adjusting hole is formed in one side of the upper surface of the movable disk (5) close to the edge, and a balance adjusting block is embedded or screwed in the balance adjusting hole.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920840216.7U CN210159617U (en) | 2019-06-05 | 2019-06-05 | High-flow high-efficiency multiphase reactor |
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| CN201920840216.7U CN210159617U (en) | 2019-06-05 | 2019-06-05 | High-flow high-efficiency multiphase reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110090613A (en) * | 2019-06-05 | 2019-08-06 | 昆明理工大学 | A kind of efficient heterophase reactor of big flow and its application |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110090613A (en) * | 2019-06-05 | 2019-08-06 | 昆明理工大学 | A kind of efficient heterophase reactor of big flow and its application |
| CN110090613B (en) * | 2019-06-05 | 2023-12-08 | 昆明理工大学 | High-flow high-efficiency multiphase reactor and application thereof |
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