CN111468047A - Continuous preparation method of aluminum sol - Google Patents
Continuous preparation method of aluminum sol Download PDFInfo
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- CN111468047A CN111468047A CN202010324511.4A CN202010324511A CN111468047A CN 111468047 A CN111468047 A CN 111468047A CN 202010324511 A CN202010324511 A CN 202010324511A CN 111468047 A CN111468047 A CN 111468047A
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- B01J13/00—Colloid chemistry, e.g. the production of colloidal materials or their solutions, not otherwise provided for; Making microcapsules or microballoons
- B01J13/0004—Preparation of sols
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
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Abstract
The invention provides a continuous preparation method of aluminum sol aiming at the problems of the preparation of the aluminum sol in the prior art, which comprises the following steps: (1) continuously reacting the sodium aluminate solution with carbon dioxide gas in a gas-liquid continuous reactor; (2) carrying out solid-liquid separation on the original slurry obtained by the reaction to obtain primary precipitate after the solid-liquid separation; (3) continuously outputting the obtained primary precipitate to a continuous pulping machine, wherein the continuous pulping machine comprises a pulping tank, and desalted water is introduced into the pulping tank for pulping and washing; (4) carrying out solid-liquid separation again to obtain a secondary precipitate after the solid-liquid separation; and (3) if the secondary precipitation meets the purity requirement of the aluminum sol product, directly outputting the aluminum sol product, otherwise, returning the secondary precipitation to the step (3), and circularly performing the steps (3) and (4) until the purity requirement of the aluminum sol product is met. The invention can realize continuous reaction, continuous separation and continuous washing, and can greatly improve the productivity and the automation degree.
Description
Technical Field
The invention belongs to the technical field of aluminum sol preparation, and particularly relates to a continuous preparation method of aluminum sol.
Background
The aluminum sol is prepared by uniformly dispersing positively charged hydrated alumina fine particles in waterThe colloidal solution of (4). The chemical formula of the aluminum sol is a (Al)2O3•nH2O)·bHx·cH2O, wherein: al2O 3. nH2O is hydrated alumina, Hx is peptizing agent, and the coefficient: b<a. c and n. The aluminum sol has the characteristics of adhesiveness, thixotropy, easy dispersibility, water solubility reversibility, suspension property, electropositivity, adsorbability, stability and the like, and is widely used as a catalyst binder and a water treatment flocculant in industry at present. The preparation method of the aluminum sol is various, and the common preparation method mainly comprises the following steps: the metal aluminum method, the organic alkoxide hydrolysis method, the electrolysis method, the inorganic salt raw material method, the powder dispersion method, and the like, wherein the inorganic salt raw material method is the method with the lowest production cost.
Metal aluminum method: the potential safety hazard is big, and the easy problem that appears falling jar, flash explosion etc. equipment life cycle is shorter. Stirring, heating, cooling and the like are required continuously in the production process, the operation conditions are complex, the energy consumption is high, and the capacity of reaction equipment is small, so that the productivity is low.
US4028216 describes in detail the preparation of metal aluminum sol at the earliest, which is simple and easy to operate, but since aluminum sol is prepared from aluminum hydroxide, the method is expensive and consumes a lot of electricity, and hydrogen generated during the preparation process also brings safety hazards and the hydrochloric acid used corrodes equipment.
The organic alkoxide hydrolysis method can prepare sol with high purity, large specific surface area and uniform particle size distribution. The method is suitable for preparing the alumina powder with high purity requirement. However, the greatest difficulty in the preparation process of the method is that the raw materials are sensitive to water, the hydrolysis reaction is very rapid, precipitates are easy to form, and the raw materials are expensive, flammable, toxic, difficult to store and bring difficulty to industrialization.
CN1177653A reports that the aluminum sol is prepared by adopting an electrolytic method, the polyaluminium chloride is synthesized by an electrochemical method with low voltage and large current, and a common anionic membrane with low price is adopted, so that the preparation cost of the product is reduced, and the method is relatively environment-friendly. However, the electrolytic water consumption is excessive, the initial cost is high (electrodes are needed in the repeating unit), chlorine gas may be generated, and potential safety hazards exist.
The alumina sol prepared by the powder dispersion method omits a hydrolysis step, the process is simple, and the raw materials are industrial products, so that the storage is convenient, and the industrialization is easy to realize. However, the SB powder in the raw material is expensive, the raw material often contains impurities, and the purity of the prepared alumina sol is relatively low.
Disclosure of Invention
The invention provides a continuous preparation method of aluminum sol, aiming at the problems in the prior art, which can greatly improve the productivity and the automation degree through continuous reaction, continuous separation and continuous washing.
The invention adopts the following technical scheme:
the continuous preparation method of the aluminum sol comprises the following steps:
(1) adding a sodium aluminate solution into a gas-liquid continuous reactor, and then introducing carbon dioxide gas for reaction, wherein the gas inlet speed of the carbon dioxide gas is based on the discharging pH value at the reaction end point, and the discharging pH value at the reaction end point is 9-12;
(2) when the requirement of the reaction end point is met, the gas-liquid continuous reactor continuously outputs the obtained original slurry to a primary centrifuge for solid-liquid separation, and primary precipitation and primary wastewater are obtained after the solid-liquid separation; the primary wastewater can be directly discharged;
(3) continuously outputting the obtained primary precipitate to a continuous pulping machine, wherein the continuous pulping machine comprises a pulping tank, desalted water is introduced into the pulping tank, and the primary precipitate is stirred and dispersed in the pulping tank under the action of the desalted water to form primary slurry;
the continuous pulping machine is obtained by modifying an SF type flotation machine, and the specific modification comprises the following two aspects: (a) removing a scraper of the SF type flotation machine; (b) an overflow port is arranged at the upper part of the slurry melting tank wall of the SF type flotation machine, and the overflow port is preferably arranged at 7/8 which is the height of the slurry melting tank wall; in addition, the discharge hole of the primary centrifugal machine is communicated to the top of the slurry melting tank through a pipeline, namely, the feed inlet of the slurry melting tank is positioned at the top of the slurry melting tank, and the demineralized water is also communicated to the top of the slurry melting tank through a pipeline, namely, the water inlet of the slurry melting tank is positioned at the top of the slurry melting tank;
(4) the upper part of the slurry melting tank is provided with an overflow port, the primary slurry is continuously output into a buffer tank through the overflow port, the buffer tank continuously outputs the primary slurry into a secondary centrifuge for solid-liquid separation again, and secondary precipitation and secondary wastewater are obtained after the solid-liquid separation; directly discharging secondary wastewater; and (3) if the secondary precipitation meets the purity requirement of the aluminum sol product, directly outputting the aluminum sol product, otherwise, returning the secondary precipitation to the step (3), and circularly performing the steps (3) and (4) until the purity requirement of the aluminum sol product is met.
In the invention, the primary centrifugal machine and the secondary centrifugal machine are not particularly limited, and the requirement of centrifugal separation of solid and liquid can be met.
In actual production, the technicians in the field can reasonably control the feed flow rate of the sodium aluminate, the feed flow rate of the primary horizontal centrifuge, the slurry feed flow rate and the feed flow rate of the secondary horizontal centrifuge in combination with the working conditions on site to ensure that the whole production process continuously and smoothly runs, and preferably, in the step (1), the concentration of the sodium aluminate solution is 20-80 g/L.
Preferably, in step (1), the reaction temperature is 15-65 ℃.
Preferably, in the step (1), the purity of the carbon dioxide gas is 99% or more.
The traditional inorganic salt raw material method has the advantages that the raw materials used by the traditional inorganic salt raw material method are low in price, the method is simple, the production cost of the aluminum sol is reduced, but the purity of the sol is low, the main reason is that the aluminum sol is a colloidal solution formed by uniformly dispersing hydrated alumina fine particles in water, the aluminum sol is difficult to separate from a reacted salt solution, so that the aluminum sol adsorbs metal cations of the salt solution after the reaction, and the aluminum sol cannot be washed and filtered due to the difficulty in separation.
The structure of the gas-liquid continuous reactor used in step (1) of the present invention is explained below:
the top and the bottom of the gas-liquid continuous reactor are respectively provided with a feeding pipeline and a discharging pipeline, the bottom of the reactor is also provided with an air inlet pipeline, the air inlet pipeline is positioned above the discharging pipeline, a plurality of gas distribution discs are distributed in the reactor along the direction of a central axis, the plane where the gas distribution discs are positioned is perpendicular to the direction of the central axis of the reactor, a plurality of vent holes are distributed in the gas distribution discs, a stirring shaft is also arranged in the reactor along the direction of the central axis, the center of each gas distribution disc is provided with a perforation, the stirring shaft sequentially penetrates through the perforation, the stirring shaft is provided with a plurality of stirring paddles along the direction of the central axis, and the stirring paddles are close to the gas distribution discs. Wherein, one end of the stirring shaft extends into the reactor and is connected to the motor so as to drive the stirring shaft to rotate.
According to the invention, the feeding pipeline is used for inputting reaction liquid of sodium aluminate and the like from top to bottom, the gas inlet pipeline is used for inputting mixed gas of carbon dioxide and air from bottom to top, the reaction liquid and the gas are in countercurrent contact reaction, and the gas distribution plate preferably covers the whole cross section inside the reactor so as to obtain the optimal gas scattering effect.
The structure of the reactor is not particularly limited, and the reactor can be realized by common reaction towers, reaction kettles and the like, and the preferable reactor structure is a rotor shape.
The shape of the stirring paddle is not particularly limited, the stirring requirement is met, the stirring diameter of the stirring paddle is 4/5 of the inner diameter of the reactor, and the mixing effect is good. Preferably, the stirring paddle is inclined by 45 degrees relative to the plane of the gas distribution plate, so that the mixing of the reaction liquid and the gas can be realized in a higher spatial range.
According to the invention, the gas distribution plate is preferably fixed in the following way: the circumferential edge of the gas distribution plate is fixedly connected with the inner wall of the reactor.
In the present invention, the gas distribution plate is mainly used for scattering and distributing gas, the stirring paddle is mainly used for stirring the flow of the reaction liquid, the two are complementary to each other to realize the mixing reaction of the gas and the reaction liquid, the specific number of the gas distribution plate or the stirring paddle is not limited in the present invention, but the following design is preferred in the present invention in view of the mixing effect: the number of the stirring paddles is the same as that of the gas distribution discs.
In order to facilitate the emptying of materials, the bottom of the reactor is a conical bottom, and the cone angle of the conical bottom is 45 ℃; meanwhile, considering factors such as the mixing process of materials, the height-diameter ratio of the reactor is preferably 6-8: 1.
According to production practice, the pseudoboehmite generated in the reactor is easy to adhere and scar, and for this reason, the inner wall of the reactor, the stirring shaft and the stirring paddle are all made of polytetrafluoroethylene.
Firstly, the invention adds a plurality of layers of gas distribution discs and stirring slurry, a plurality of air holes distributed on the gas distribution discs uniformly distribute and scatter gas input from the bottom, and simultaneously, the stirring action of the stirring slurry is assisted, thus effectively preventing laminar flow generated in the reaction process, solving the problem of uneven reaction of the traditional batch reactor, realizing continuous reaction of sodium aluminate and carbon dioxide through a continuous gas-liquid reactor, continuously and rapidly reacting to generate alumina sol, realizing continuous preparation of the original alumina sol slurry, immediately carrying out continuous primary solid-liquid separation through a centrifuge, carrying out slurry washing on the separated alumina sol in a continuous slurry machine by using desalted water added with an ion exchanger, then carrying out continuous secondary solid-liquid separation, and repeating the steps of slurry washing and secondary separation according to the purity requirement of the alumina sol. The invention has the advantages that the pulping machine in the prior art can only carry out intermittent pulping operation and cannot meet the requirement of continuous pulping, and therefore, the invention discovers that the SF type flotation machine can realize the function of continuous pulping after being slightly modified (no flotation function exists), so that the modified SF type flotation machine is adopted as the continuous pulping machine for use, the aluminum sol can be continuously separated and washed, the repetition times of the steps (3) and (4) are selected according to different purity requirements of the aluminum sol, and the invention benefits from continuous operation of continuous reaction, continuous separation and continuous washing, has flexible operation and simple control, and greatly improves the productivity and the automation degree of enterprises.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly introduced below, it is obvious that the drawings in the following description are only some embodiments described in the present application, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts;
FIG. 1 is a front view of a gas-liquid continuous reactor in example 1;
FIG. 2 is a left side view of a gas-liquid continuous reactor in example 1;
FIG. 3 is a plan view of a gas-liquid continuous reactor in example 1;
FIG. 4 is a schematic view showing the internal structure of a gas-liquid continuous reactor in example 1;
FIG. 5 is a schematic flow chart of the present invention;
in the figure, 1, a reactor; 2. a feed conduit; 3. an air intake duct; 4. a discharge pipeline; 5. a feed control valve; 6. an air intake control valve; 7. an evacuation valve; 8. a support leg; 9. an overflow port; 10. a gas distribution plate; 11. a stirring shaft; 12. stirring the slurry;
200. a first-stage horizontal centrifuge; 300. continuously pulping; 400. a buffer tank; 500. a two-stage horizontal centrifuge.
Detailed Description
In order to make the technical purpose, technical solutions and advantages of the present invention clearer, the technical solutions of the present invention are further described below with reference to the accompanying drawings and specific embodiments.
In the description of the present invention, "a plurality" means two or more unless otherwise specified; the terms "upper", "lower", "left", "right", "inner", "outer", "front", "rear", "head", "tail", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, are only for convenience in describing and simplifying the description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed in a particular orientation, and be operated, and thus, should not be construed as limiting the invention. Furthermore, the terms "first," second, "" third, and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected" and "connected" are to be interpreted broadly, e.g., as being fixed or detachable or integrally connected; can be mechanically or electrically connected; may be directly connected or indirectly connected through an intermediate. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
The method comprises the steps of carrying out continuous slurry separation in a reactor 1 at a capacity of 2m, conveying 30 g/L of sodium aluminate solution into the reactor 1 at a feeding speed of 1m, introducing carbon dioxide gas with a purity of 99% or more at a temperature of 45 ℃, controlling the gas inlet speed of the carbon dioxide gas based on the discharge pH value of 11 +/-0.2, when the discharge requirement is met, conveying aluminum sol original slurry to a primary horizontal centrifuge 200 by the reactor, controlling the highest rotation speed of 3000-class slurry/min (adjustable) of the primary horizontal centrifuge 200 at 2500-class, controlling the separation factor at 3500, 250-450mm in the diameter of a rotary drum and 1000-2000mm in the length of the rotary drum, conveying the primary precipitate into a continuous slurry mixer 300 through a pipeline after solid-liquid separation, separating the primary precipitate and primary wastewater, discharging the primary wastewater, controlling the content of alumina in the primary precipitate to 23-25%, conveying the primary precipitate into a secondary slurry mixer through a continuous slurry mixer 300, and a scrubbing machine 300 for washing, and discharging the secondary slurry from the primary precipitate, and the secondary slurry mixer after solid-liquid separation, wherein the primary precipitate is discharged through a secondary slurry mixer, the secondary slurry mixer is used for discharging the secondary slurry mixer after the primary precipitate, the primary slurry mixer, the secondary slurry mixer is used for discharging the secondary slurry separation, and the secondary slurry mixer for discharging the secondary slurry from the secondary slurry mixer, the secondary slurry mixer after the primary slurry mixer, the secondary slurry mixer is used for discharging the secondary slurry mixer, and the secondary slurry mixer, wherein the secondary slurry is used for discharging the secondary slurry from the secondary slurry mixer, the secondary slurry mixer for discharging of the secondary slurry separator for discharging the secondary slurry separation, the secondary slurry separator for discharging of the secondary slurry separator under the secondary slurry separator for discharging of the secondary slurry from the secondary slurry separator under the secondary.
Wherein, serialization pulp grinder is transformed by SF type flotation device and is obtained, and the specific transformation includes following two aspects: (1) removing a scraper of the SF type flotation machine; (2) an overflow port is arranged at the upper part of the slurry melting tank wall of the SF type flotation machine, and the overflow port is preferably arranged at 7/8 which is the height of the slurry melting tank wall; in addition, the discharge hole of the primary centrifugal machine is communicated to the top of the slurry melting tank through a pipeline, namely, the feed inlet of the slurry melting tank is positioned at the top of the slurry melting tank, and the demineralized water is also communicated to the top of the slurry melting tank through a pipeline, namely, the water inlet of the slurry melting tank is positioned at the top of the slurry melting tank;
in the embodiment, after continuously running for 1h, 2h and 3h, sampling analysis is carried out on the alumina sol and the secondary wastewater which are obtained by solid-liquid separation after pulping and washing for three times, wherein the content of sodium oxide in the secondary wastewater is 0.042%, 0.039% and 0.040%, the content of alumina in the alumina sol is 24.3%, 24.6% and 24.5%, and the whole operation is stable; in long-time production operation, the separated washing wastewater can be sampled at regular time, and the quality of the aluminum sol can be judged by analyzing the content of sodium oxide.
In this embodiment, in consideration of the actual situation in the production, the separation design capacity of the centrifuge has a margin of 30%, for example, when the feed flow rate of the first-stage centrifugal separation, the reaction feed flow rate, and the slurry feed flow rate fluctuate, the feed flow rate of the next stage or the previous stage can be adjusted according to the actual flow rate of the link where the fluctuation occurs, so that the whole production process can be performed stably and orderly. For example, the reaction feeding amount or the first-stage centrifugal separation feeding amount is increased or decreased, and the flow can be correspondingly increased or decreased in the subsequent slurry feeding link. If washing fluctuation occurs, the content of sodium oxide is increased, the reaction feeding amount is reduced, the subsequent flow rate is kept unchanged, or the water inlet flow rate of the desalted water and the slurry feeding amount are increased, so that the quality of the aluminum sol is stabilized.
The structure of the gas-liquid continuous reactor selected in this example is described below: as shown in fig. 1 to 4, in the gas-liquid continuous reactor, the whole reactor 1 is cylindrical, the bottom of the reactor 1 is a conical bottom, the cone angle of the conical bottom is 45 ℃, the inner diameter of the reactor 1 is preferably 0.3 to 2m, the reactor 1 is designed to be 1.5m in this embodiment, the height of the reactor 1 is 9m, the bottom of the conical bottom of the reactor 1 is communicated with an evacuation pipeline, and an evacuation valve 7 is arranged on the evacuation pipeline, so that when the reactor needs to be cleaned, the residual materials in the reactor are evacuated.
The top and the bottom of the reactor 1 are respectively provided with a feeding pipeline 2 and a discharging pipeline 4, the bottom of the reactor 1 is also provided with an air inlet pipeline 3, the air inlet pipeline 3 is positioned above the discharging pipeline 4, the feeding pipeline 2 is provided with a feeding control valve 5, the air inlet pipeline 3 is provided with an air inlet control valve 6, and the feeding control valve 5 and the air inlet control valve 6 are in interlocking design so as to control the volume ratio of the flow rate of the reaction liquid to the flow rate of the gas to be 1: 50-150; three layers of gas distribution discs 10 are uniformly distributed in the reactor 1 along the central axis direction, the plane of the gas distribution discs 10 is perpendicular to the central axis direction of the reactor 1, a plurality of vent holes are densely distributed in the gas distribution discs 10, the diameter of each vent hole is 3cm, and the distance between the centers of circles of adjacent vent holes is 7 cm; still be equipped with (mixing) shaft 11 along the central axis direction in the reactor 1, the center of gas distribution dish 10 is equipped with the perforation, (mixing) shaft 11 passes in proper order the perforation sets up, (mixing) shaft 11 is equipped with three stirring thick liquid 12 along the central axis direction, stirring thick liquid 12 is close to gas distribution dish 10 sets up, specifically, and the stirring thick liquid 12 that is located the top sets up in the below that is located the gas distribution dish 10 of the top, and the stirring thick liquid 12 that is located the centre sets up in the top that is located middle gas distribution dish 10, and the stirring thick liquid 12 that is located the below sets up in the top that is located the gas distribution dish 10 of the bottom, furtherly, stirring shaft 11 extends to the 5cm department in the top that is located the gas distribution dish 10 of.
In this embodiment, the diameter of the inlet pipeline 3 is 40-80cm, the diameter of the inlet pipeline is 40-80cm, and the diameter of the outlet pipeline 4 is 80-120 cm.
In this example, the stirring diameter of the stirring paddle 12 is 4/5, i.e., 1.2m, of the inner diameter of the reactor 1. Preferably, the plane formed by the rotation of the stirring paddle 12 is arranged at an angle of 45 ° with respect to the plane of the gas distribution plate 10, and the rotation speed is designed to be 40-400 rpm.
In this embodiment, the circumferential edge of the gas distribution plate 10 is fixedly connected to the inner wall of the reactor 1.
In this embodiment, the inner wall of the reactor 1, the stirring shaft 11 and the stirring paddle 12 are all made of polytetrafluoroethylene, so that the scab phenomenon occurring in the process of generating solids through gas-liquid reaction is reduced.
Finally, it should be noted that: the above embodiments are merely illustrative and not restrictive of the technical solutions of the present invention, and any equivalent substitutions and modifications or partial substitutions made without departing from the spirit and scope of the present invention should be included in the scope of the claims of the present invention.
Claims (10)
1. The continuous preparation method of the aluminum sol is characterized by comprising the following steps:
(1) adding a sodium aluminate solution into a gas-liquid continuous reactor, and then introducing carbon dioxide gas for reaction, wherein the gas inlet speed of the carbon dioxide gas is based on the discharging pH value at the reaction end point, and the discharging pH value at the reaction end point is 9-12;
(2) when the requirement of the reaction end point is met, the gas-liquid continuous reactor continuously outputs the obtained original slurry to a primary centrifuge for solid-liquid separation, and primary precipitation and primary wastewater are obtained after the solid-liquid separation;
(3) continuously outputting the obtained primary precipitate to a continuous pulping machine, wherein the continuous pulping machine comprises a pulping tank, desalted water is introduced into the pulping tank, and the primary precipitate is stirred and dispersed in the pulping tank under the action of the desalted water to form primary slurry;
(4) the upper part of the slurry melting tank is provided with an overflow port, the primary slurry is continuously output into a buffer tank through the overflow port, the buffer tank continuously outputs the primary slurry into a secondary centrifuge for solid-liquid separation again, and secondary precipitation and secondary wastewater are obtained after the solid-liquid separation; and (3) if the secondary precipitation meets the purity requirement of the aluminum sol product, directly outputting the aluminum sol product, otherwise, returning the secondary precipitation to the step (3), and circularly performing the steps (3) and (4) until the purity requirement of the aluminum sol product is met.
2. The continuous preparation method of alumina sol according to claim 1, wherein in step (1), the concentration of the sodium aluminate solution is 20 to 80 g/L.
3. The continuous production method of an aluminum sol according to claim 1, wherein the reaction temperature in the step (1) is 15 to 65 ℃.
4. The continuous production method of an aluminum sol according to claim 1, wherein the purity of the carbon dioxide gas in the step (1) is 99% or more.
5. The continuous production method of aluminum sol according to claim 1, wherein in the step (3), the demineralized water is an aqueous solution of an ion exchanger, and the concentration of the ion exchanger is 0.08 to 0.15 g/L.
6. The continuous production method of aluminum sol according to claim 1, wherein in the step (1), the top and the bottom of the gas-liquid continuous reactor are respectively provided with a feeding pipeline and a discharging pipeline, the bottom of the reactor is also provided with an air inlet pipeline, the gas inlet pipeline is positioned above the discharge pipeline, a plurality of gas distribution discs are distributed in the reactor along the direction of the central axis, the plane of the gas distribution plate is vertical to the direction of the central axis of the reactor, a plurality of vent holes are distributed on the gas distribution plate, a stirring shaft is arranged in the reactor along the direction of the central axis, the center of the gas distribution plate is provided with a through hole, the (mixing) shaft passes in proper order the perforation sets up, the (mixing) shaft is equipped with a plurality of stirring thick liquids along the central axis direction, the stirring thick liquid is close to the gas distribution dish sets up.
7. The continuous production method of aluminum sol according to claim 6, wherein the stirring diameter of the stirring blade is 4/5 degrees of the inner diameter of the reactor, and the stirring blade is inclined at 45 degrees with respect to the plane of the gas distribution plate.
8. The continuous preparation method of aluminum sol according to claim 6, wherein the circumferential edge of the gas distribution plate is fixedly connected with the inner wall of the reactor, and the number of the stirring paddles is the same as the number of the gas distribution plate.
9. The continuous preparation method of aluminum sol according to claim 6, wherein the bottom of the reactor is a conical bottom, the cone angle of the conical bottom is 45 ℃, and the aspect ratio of the reactor is 6-8: 1.
10. The continuous production method of aluminum sol according to claim 6, wherein the inner wall of the reactor, the stirring shaft and the stirring paddle are made of polytetrafluoroethylene.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114522632A (en) * | 2020-11-06 | 2022-05-24 | 中国石油化工股份有限公司 | Preparation device and preparation method of pseudo-boehmite |
| RU2816710C1 (en) * | 2023-06-06 | 2024-04-03 | Общество с ограниченной ответственностью "Объединенная Компания РУСАЛ Инженерно-технологический центр" | Method of sub-sludge water treatment |
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| RU2816710C1 (en) * | 2023-06-06 | 2024-04-03 | Общество с ограниченной ответственностью "Объединенная Компания РУСАЛ Инженерно-технологический центр" | Method of sub-sludge water treatment |
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Application publication date: 20200731 |