CN102838148A - Reactor and method used for preparing aluminum hydroxide - Google Patents
Reactor and method used for preparing aluminum hydroxide Download PDFInfo
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- CN102838148A CN102838148A CN201110169570XA CN201110169570A CN102838148A CN 102838148 A CN102838148 A CN 102838148A CN 201110169570X A CN201110169570X A CN 201110169570XA CN 201110169570 A CN201110169570 A CN 201110169570A CN 102838148 A CN102838148 A CN 102838148A
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Abstract
The invention discloses a reactor and a method used for preparing aluminum hydroxide. The reactor employs a self-priming stirrer assembly which is mainly composed of a rotor and a stator. The rotor employs a closed backward-curved flow-channel impeller. The rotor is fixed on a stirring shaft. Deflector vanes are arranged in the stator. Compared with prior arts, when the reactor provided by the invention is used for carrying out a carbonization reaction, because gas is absorbed automatically during a stirring process, no gas compressor is needed, such that power and investment are saved. With the self-priming stirring of the rotor and the guiding function of the stator, gas bubbles produced after gas distribution have small sizes, and gas utilization rate is increased by 1 time or higher. Prepared aluminum hydroxide dry gum grains have uniform sizes and centralized pore size distribution. With the rotation of the rotor, the shearing action upon fluid is small, such that the sizes of the prepared aluminum hydroxide dry gum grains are not affected by the shearing action.
Description
Technical field
The present invention relates to a kind of reactor drum and method for preparing white lake, more particularly, relate to a kind of reactor drum and method with Carbonization Preparation white lake.
Background technology
Activated alumina refers generally to γ-Al
2O
3,, surface chemistry stronger than higher specific surface area, adsorptivity, certain porosity and pore size distribution are arranged, commonly usedly make the support of the catalyst in the petrochemical complex industry.γ-Al
2O
3Usually get by pseudo-boehmite roasting at high temperature.
The method of producing pseudo-boehmite is a lot, is divided into aluminium alcoholates hydrolysis method and neutralisation generally.Adopt the reaction of sodium aluminate solution and carbonic acid gas (carborization) to generate the method for intending thin aluminium stone; Can be regarded as and adopt the neutralisation of carbonic acid gas as acid source, carborization production to intend thin aluminium stone because of raw material sources convenience, production process " environmental protection ", with low cost being used widely.
CN1212237A discloses a kind of method of preparing active aluminum oxide by sodium aluminate carbonating process; By become glue, aging, washing, filter, dry, calcination steps forms; It becomes the glue process to adopt the disclosed novel reactor that is used to prepare white lake of CN2264173A; This reactor drum replaces mechanical stirring with the gas bubbling, and gas distribution grid is equipped with in the junction at the bottom of the tower body of reactor drum and tower, and the aperture area diameter of gas distribution grid equals the diameter of tower body.And the disclosed novel reactor that is used to prepare white lake of CN2616525A improves above-mentioned reactor drum, increased the gas distribution grid of gas quadratic distribution, improved the stirring efficiency of gas effciency and reactor drum.
Above-mentioned two kinds of reactor drums have been avoided the shortcoming that traditional mechanical stirred reactor energy consumption is big, gas distribution is uneven, utilization ratio is low to a certain extent, but also have disadvantage:
1, need synergic system that the CO of certain pressure is provided
2Or CO
2Gas mixture;
2, gas distribution tube and grid distributor are prone to stopped up by resultant, the cleaning difficulty;
3, after the gas distribution, bubble size is still bigger, and gas effciency also remains further to be improved;
4, the aluminum hydroxide grain of preparation size heterogeneity, the pore size distribution disperse.
Summary of the invention
In order to overcome above-mentioned weak point of the prior art, the invention provides and a kind ofly need not higher intake pressure, gas distribution is even, bubble size is little, gas distributor is difficult for stopping up and the reactor drum and the method for the preparation white lake that gas effciency is high.Adopt this reactor drum gained aluminum hydroxide grain size homogeneous, pore size distribution to concentrate.
The present invention prepares the reactor drum of white lake, comprises reactor body, opening for feed, inlet mouth, venting port, agitator assembly, and wherein agitator assembly is the hollow agitator assembly; This assembly is contained in the reactor body, is provided with stator, rotor, intake hood, stir shaft, and described rotor adopts sealing palintrope flow channel type impeller; Rotor is fixed on the stir shaft, and through the outer driver drives rotor rotation of reactor body, stator is an immobilized; Be fixed on the reactor body, the water conservancy diversion fin is housed in the stator, intake hood is located at rotor top; Link to each other with the stator top is airtight, intake hood is provided with pneumatic outlet, and stator and rotor coaxial are installed; Leave spacing between stator and rotor, stator inlet mouth and rotor air outlet are radially relative, and rotor inlet mouth and intake hood outlet are axially relatively.
The present invention prepares the reactor drum of white lake, and the diameter of its rotor 5 is 1/2 ~ 1/30 of reactor body 9 diameters, and preferred version is 1/3 ~ 1/15.Stator 4 external diameters are 1.5 ~ 4.0 times of rotor 5 diameters, are preferably 2.0 ~ 3.0 times.The spacing of stator 4 and rotor 5 is 0.5 ~ 5.0mm, is preferably 1.0 ~ 2.5mm.The rotating speed of rotor 5 is 200 ~ 5000 rev/mins, is preferably 500 ~ 3000 rev/mins.The water conservancy diversion fin is 15 ° ~ 60 ° with angle radially, is preferably 25 ° ~ 45 °.8 ° ~ 80 ° of blade 11 digressions of palintrope flow channel type impeller are preferably 15 ° ~ 50 °.The quantity of water conservancy diversion fin is 3 ~ 20, is preferably 6 ~ 16.Impeller vane quantity is 2 ~ 8, is preferably 4 ~ 8.
The preparation method of white lake of the present invention, process comprises: sodium aluminate solution contacts in above-mentioned reactor drum with carbonated gas, prepares the pseudo-boehmite gel with the carburizing reagent mode, obtains white lake then.
The preparation method of white lake of the present invention, specific as follows:
(1), prepares sodium aluminate solution, with Al
2O
3Meter concentration is 10～60g/1000mL, preferably is controlled at 25～35g/1000mL;
(2), add in above-mentioned reactor drum and submergence rotor by opening for feed sodium aluminate solution; Start operation reactor drum; Treat that wheel speed reaches 200～5000 rev/mins, be preferably in 500～3000 rev/mins after, in reactor drum, feeding volumetric concentration by inlet mouth is 50% ~ 98% CO
2Gas, reactor temperature are controlled at 4 ~ 50 ℃, preferably are controlled at 15～35 ℃, and the pH value of solution reaches 9.5 ~ 11.5 in reactor drum, are preferably at 10.0～10.5 o'clock and stop to feed CO
2Gas, wear out in rotating speed to 100 ~ 800 rev/min that reduce impeller;
(3), the slurries of step (2) gained are taken out in reactor drum, through filtration, washing and drying process, obtain aluminum hydroxide solid elastomer.
The described aging condition of step (2) is following: aging temperature is controlled at 4 ~ 50 ℃, preferably is controlled at 15～35 ℃, and digestion time is 10～60 minutes, is preferably 30～40 minutes.
The described washing of step (3) is the cakes with deionized water washing that filtration is obtained, and when the deionized water pH value of washing reached 7.0～7.5, washing finished; Described drying conditions is following: 100 ~ 150 ℃ of dryings 6 ~ 12 hours, obtain aluminum hydroxide solid elastomer.
The present invention prepares the hollow agitator assembly of white lake reactor drum and mainly is made up of rotor and stator, and rotor is by the stir shaft drive of whipped-up structure down.With sodium aluminate solution pack into reactor drum and submergence rotor, because the rotor high-speed rotation, liquids and gases are under action of centrifugal force; Be thrown toward the impeller edge, in this process, fluid just obtains energy; If the rotating speed of rotor is faster, impeller edge line speed is also bigger, and then fluidic kinetic energy is also bigger; After fluid leaves rotor, change pressure into by kinetic energy and can also heal greatly, the tolerance of discharge is also big more.
When the fluid in the rotor cavity when the center is thrown toward outer rim, form negative pressure at the rotor center place, rotor speed is bigger; The negative pressure that is caused is bigger, because the cavity of rotor communicates with intake hood, therefore; Gas constantly is inhaled into, and gets rid of to the impeller edge, through the water conservancy diversion fin gas-liquid uniform distribution is thrown away; Because the stirring action of rotor, gas-liquid forms mixed flow (turbulent flow) around impeller, makes the gas that just leaves impeller constantly split into trickle bubble in the round-robin solution immediately; And under turbulence state, mix, seethe, be diffused in the whole reactor, so the self-priming stirring system has been accomplished aeration when stirring.
Rotor adopts the single suction inclosed impeller, and impeller is the palintrope runner.Compare with the radial flow path shape with antecurvature, the palintrope runner is long, and under the situation that the runner exit area equates, the runner diffusion is little and level and smooth, and resistance is little, has reduced the fluidic shearing action.
Because the gas that is sucked by rotor forms small bubble, make evenly contact closely of gas-liquid, the gas-to-liquid contact surface is brought in constant renewal in, and has improved mass-transfer efficiency, has improved the utilization ratio of gas.Again because rotor and stator are cavity structure, and have gas-liquid to pass through at a high speed, so be difficult for having obstruction herein, Liquid Flow is unobstructed.
Compared with prior art, the present invention has following advantage: adopt this reactor drum to carry out carburizing reagent, owing in whipping process, suck gas certainly, the undesirable gas compressor is saved power and investment; Because the self-priming of rotor stirs and the guide effect of stator, makes the bubble size that produces after the gas distribution very little, gas effciency is enhanced about more than once.Have aperture gas distribution tube and grid distributor owing to having cancelled again, fluid is bigger through the sectional dimension in path, is difficult for producing latch up phenomenon; Do not need cleaning, improved the safety of equipment operation, reduced maintenance cost; The aluminum hydroxide solid elastomer grain size homogeneous of preparation; Pore size distribution is concentrated, and because the shearing action of the rotation convection cell of rotor is little, the aluminum hydroxide solid elastomer grain size of preparation does not receive the influence of shearing action and changes.
Reactor drum of the present invention can be applicable in the preparation process of alumina supporter.Carbonization Preparation white lake is with characteristics such as its operational path are simple, with low cost, equipment requirements is low and pollution-free; Have a extensive future, reactor drum of the present invention is applied to catalyst manufacturer, can enhance productivity; Save facility investment, reduce maintenance cost.
Description of drawings
Fig. 1 is a structure of reactor synoptic diagram of the present invention;
Fig. 2 is reactor drum stator of the present invention and rotor structure synoptic diagram;
Fig. 3 is reactor drum stator of the present invention and rotor structure transverse cross-sectional view
Fig. 4 is the pore distribution of the embodiment of the invention and comparative example gained aluminum oxide;
Fig. 5 is the size distribution of the embodiment of the invention and comparative example gained aluminum oxide;
1. reactor evacuated mouths among the figure; 2. reactor drum inlet mouth; 3. intake hood; 4. stator; 5. rotor; 6. drive and tightness system; 7. reactor feed mouth; 8. rotor inlet mouth; 9. reactor body; 10. water conservancy diversion fin; 11. blade.
Embodiment
Below in conjunction with accompanying drawing the present invention is described in further detail.
Structure of reactor of the present invention is as shown in Figure 1; Reactor drum mainly is made up of reactor body 9, reactor feed mouth 7, inlet mouth 2, driving and tightness system 6, venting port 1, hollow agitator assembly, and wherein the hollow agitator assembly is made up of intake hood 3, stator 4, rotor 5, stir shaft.Stir shaft is driven rotor 5 and is rotated by the driver drives outside the reactor body 9.Intake hood 3 is airtight the connection with stator 4, can adopt also sealable the living of sealing welding process to connect.
Rotor 5 as shown in Figure 2 adopts closed palintrope flow channel type impeller.Water conservancy diversion fin 10 is housed in the stator 4, and water conservancy diversion fin 10 forms airtight passage with the upper and lower cover plate of stator 4, has prolonged the path of Liquid Flow, has increased gas-liquid contact time, helps improving gas effciency.Water conservancy diversion fin 10 with certain angle is radially arranged.The inlet mouth 8 of rotor 5 is directly relative with intake hood 3 outlets, and when rotor 5 rotated, gas got in the rotors 5 through inlet mouth 2, intake hood 3, after stator 4 gets in the reactor body 9.Solution in the reactor body 9 gets into stator 4 by the gap between stator 4 and the rotor 5; Gas-liquid is discharged the back from stator 4 passages and reactor body 9, has also been played the effect of liquid in the stirred reactor; The small bubble of rotor 5 generations meanwhile rises in reactor body 9 and continues to accomplish gas liquid reaction, and last residual gas is discharged outside the reactor drum through reactor body venting port 1.The diameter of rotor 5 is 1/2 ~ 1/30 of reactor body 9 diameters, and preferred version is 1/3 ~ 1/15.Stator 4 external diameters are 1.5 ~ 4.0 times of rotor 5 diameters, are preferably 2.0 ~ 3.0 times.The spacing of stator 4 and rotor 5 is 0.5 ~ 5.0mm, is preferably 1.0 ~ 2.5mm.The rotating speed of rotor 5 is 200 ~ 5000 rev/mins, is preferably 500 ~ 3000 rev/mins.Water conservancy diversion fin 10 is 15 ° ~ 60 ° with angle radially, is preferably 25 ° ~ 45 °.8 ° ~ 80 ° of the blade digressions of palintrope flow channel type impeller are preferably 15 ° ~ 50 °.The quantity of water conservancy diversion fin 10 is 3 ~ 20, is preferably 6 ~ 16.Impeller vane 11 quantity are 2 ~ 8, are preferably 4 ~ 8.
Compared with prior art, adopt reactor drum provided by the invention, be used for the one-tenth glue process of white lake, device undesirable gas compressor is to gas boosting, and DESIGN OF REACTOR pressure reduces greatly, saves power and investment; Because the intake pressure that needs is less, DESIGN OF REACTOR pressure is reduced, and be easy to maximize.The bubble size that produces after the gas distribution is very little, reaches below the 0.1mm, and gas effciency is enhanced about more than once, and the reaction times shortens over half.And be difficult for producing the phenomenon that resultant stops up gas distributor, reduced maintenance cost, improved the safety of equipment operation, prolonged the turnaround of equipment greatly.
Further specify the present invention below in conjunction with embodiment.
Embodiment adopts reactor drum of the present invention, and the diameter of its rotor 5 is 1/8 of reactor body 9 diameters.Stator 4 external diameters are 2.5 times of rotor 5 diameters.The spacing of stator 4 and rotor 5 is 1.5mm.Water conservancy diversion fin 10 is 30 ° with angle radially.25 ° of the blade digressions of palintrope flow channel type impeller.The quantity of water conservancy diversion fin 10 is 16.Impeller vane quantity is 6.
Preparation is with Al
2O
3Meter concentration is the sodium aluminate solution of 25g/1000mL and adds in the reactor drum of the present invention, start operation reactor drum, treat that wheel speed reaches 500 rev/mins after, in reactor drum, feed volumetric concentration and be 55% CO
2Gas, reactor temperature are controlled at 30 ℃, when the pH of solution in reactor drum value reaches 10.5, stop to feed CO
2Gas reduces the rotating speed to 200 rev/min of impeller, carries out weathering process, and aging temperature is controlled at 30 ℃, and digestion time is 40 minutes.In reactor drum, take out dope filtration behind the aging result, cakes with deionized water is washed to pH value=7.0 and is finished, and filter cake promptly got aluminum hydroxide solid elastomer A of the present invention down in dry 10 hours at 110 ℃.At 550 ℃ of roastings sampling analysis after 4 hours, gained aluminum oxide character is seen table 1 with the gained aluminum hydroxide solid elastomer, and pore size distribution is seen Fig. 4, and gained aluminum oxide size distribution is seen Fig. 5.
Preparation is with Al
2O
3Meter concentration is the sodium aluminate solution of 35g/1000mL and adds in the reactor drum of the present invention, start operation reactor drum, treat that wheel speed reaches 3000 rev/mins after, in reactor drum, feed volumetric concentration and be 90% CO
2Gas, reactor temperature are controlled at 18 ℃, when the pH of solution in reactor drum value reaches 10.0, stop to feed CO
2Gas reduces the rotating speed to 800 rev/min of impeller, carries out weathering process, and aging temperature is controlled at 18 ℃, and digestion time is 30 minutes.In reactor drum, take out dope filtration behind the aging result, cakes with deionized water is washed to pH value=7.5 and is finished, and filter cake promptly got aluminum hydroxide solid elastomer B of the present invention down in dry 6 hours at 150 ℃.At 550 ℃ of roastings sampling analysis after 4 hours, gained aluminum oxide character is seen table 1 with the gained aluminum hydroxide solid elastomer, and pore size distribution is seen Fig. 4, and gained aluminum oxide size distribution is seen Fig. 5.
Comparative example 1
Comparative example is the dried glue of commercial alumina; This aluminum oxide preparation is to adopt in the carbonic acid gas and sodium metaaluminate; Dioxide gas adopts the bubbling form to get into reactor drum, and promptly gas distribution grid is equipped with in the junction at the bottom of the tower body of reactor drum and tower, and gas reacts through grid distributor entering reactor drum.Commercial alumina is numbered C, and its character is seen table 1, and pore size distribution is seen Fig. 4, and gained aluminum oxide size distribution is seen Fig. 5.
Can find out from table 1, Fig. 4; Pore volume, the specific surface area of the aluminum oxide of the prepared aluminum oxide pore volume of the present invention, specific surface area and commercially available Carbonization Preparation are suitable; But the pore size distribution of the aluminum oxide that the present invention is prepared is more concentrated than commercial alumina, simultaneously, from Fig. 5, finds out; White lake particle diameter of the present invention mainly is distributed in 5～20nm, and the size distribution of commercially available white lake then seems than disperse.
Table 1 preparation aluminum oxide character
| Numbering | A | B | C |
| Pore volume, g/mL | 0.926 | 0.924 | 0.928 |
| Specific surface area, m 2/g | 300 | 300 | 326 |
| Average pore diameter, nm | 12.3 | 12.3 | 11.4 |
Claims (15)
1. a reactor drum for preparing white lake comprises reactor body, opening for feed, inlet mouth, venting port, agitator assembly, it is characterized in that agitator assembly adopts the hollow agitator assembly; This assembly is contained in the reactor body, is provided with stator, rotor, intake hood, stir shaft, and described rotor adopts sealing palintrope flow channel type impeller; Rotor is fixed on the stir shaft, and through the outer driver drives rotor rotation of reactor body, stator is an immobilized; The water conservancy diversion fin is housed in the stator, and intake hood is located at rotor top, links to each other with the stator top is airtight; Intake hood is provided with pneumatic outlet, and stator and rotor coaxial are installed, and leave spacing between stator and rotor; Stator inlet mouth and rotor air outlet are radially relative, and rotor inlet mouth and intake hood outlet are axially relatively.
2. according to the described reactor drum of claim 1, the diameter that it is characterized in that said rotor is 1/2 ~ 1/30 of a reactor body diameter, and stator outer diameter is 1.5 ~ 4.0 times of rotor diameter; The spacing of stator and rotor is 0.5 ~ 5.0mm.
3. according to the described reactor drum of claim 1, the diameter that it is characterized in that said rotor is 1/3 ~ 1/15 of a reactor body diameter, and stator outer diameter is 2.0 ~ 3.0 times of rotor diameter; The spacing of stator and rotor is 1.0 ~ 2.5mm.
4. according to the described reactor drum of claim 1, the rotating speed that it is characterized in that said rotor is 200 ~ 5000 rev/mins.
5. according to the described reactor drum of claim 1, it is characterized in that said water conservancy diversion fin and rotor radial angle are 15 ° ~ 60 °, the quantity of water conservancy diversion fin is 3 ~ 20.
6. according to the described reactor drum of claim 1, it is characterized in that said water conservancy diversion fin and rotor radial angle are 25 ° ~ 45 °, the quantity of water conservancy diversion fin is 6 ~ 16.
7. according to the described reactor drum of claim 1, it is characterized in that 8 ° ~ 80 ° of the blade digressions of the palintrope flow channel type impeller of said rotor, impeller vane quantity is 2 ~ 8.
8. according to the described reactor drum of claim 1, it is characterized in that 15 ° ~ 50 ° of the blade digressions of the palintrope flow channel type impeller of said rotor, impeller vane quantity is 4 ~ 8.
9. the preparation method of a white lake; It is characterized in that adopting the arbitrary described reactor drum of claim 1 ~ 8; Process comprises: sodium aluminate solution contacts in above-mentioned reactor drum with carbonated gas, prepares the pseudo-boehmite gel with the carburizing reagent mode, obtains white lake then.
10. according to the described method of claim 9, it is characterized in that the preparation method of said white lake, specific as follows:
(1), prepares sodium aluminate solution, with Al
2O
3Meter concentration is 10～60g/1000mL;
(2), sodium aluminate solution is added in the above-mentioned reactor drum and the submergence rotor by opening for feed, start operation reactor drum, treat that wheel speed reaches 200～5000 rev/mins after, feeding volumetric concentration by inlet mouth is 50% ~ 98% CO
2Gas, reactor temperature are controlled at 4 ~ 50 ℃, when the pH of solution in reactor drum value reaches 9.5 ~ 11.5, stop to feed CO
2Gas, wear out in rotating speed to 100 ~ 800 rev/min that reduce impeller;
(3), the slurries of step (2) gained are taken out in reactor drum, through filter, washing and dry, obtain white lake.
11., it is characterized in that sodium aluminate solution in the step (1), with Al according to the described method of claim 10
2O
3Meter concentration is 25～35g/1000mL.
12. according to the described method of claim 10, it is characterized in that the described aging temperature of step (1) is controlled at 4 ~ 50 ℃, digestion time is 10～60 minutes.
13. according to the described method of claim 10, it is characterized in that step (2) reactor drum start operation, after wheel speed reaches 500～3000 rev/mins, feed CO
2Gas.
14., it is characterized in that step (2) temperature of reaction is 15～35 ℃ according to the described method of claim 10.
15., it is characterized in that when the pH of solution in reactor drum value reaches 10.0～10.5, stopping to feed CO in the step (2) according to the described method of claim 10
2Gas.
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|---|---|---|---|
| CN201110169570.XA CN102838148B (en) | 2011-06-23 | 2011-06-23 | Reactor and method used for preparing aluminum hydroxide |
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|---|---|---|---|
| CN201110169570.XA CN102838148B (en) | 2011-06-23 | 2011-06-23 | Reactor and method used for preparing aluminum hydroxide |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103964479A (en) * | 2013-01-28 | 2014-08-06 | 北京蓝天欣禾科技有限公司 | Nanometer aluminum hydroxide material and production process thereof |
| CN104671266A (en) * | 2013-11-28 | 2015-06-03 | 北京阳光欣禾科技有限公司 | Process for preparing ultrafine aluminum hydroxide by seed crystal precipitation method |
| CN104959091A (en) * | 2015-06-08 | 2015-10-07 | 辽宁石油化工大学 | Carbonization synthesis system and application of same in preparation of pseudo-boehmite, and preparation method for pseudo-boehmite |
| CN105417560A (en) * | 2015-11-20 | 2016-03-23 | 中石化催化剂（北京）有限公司 | Method for producing pseudo-boehmite by adopting inorganic membrane reactor |
| CN105417561A (en) * | 2015-11-20 | 2016-03-23 | 中石化催化剂（北京）有限公司 | Production device and method of aluminum hydroxide |
| CN113877513A (en) * | 2021-11-15 | 2022-01-04 | 成都阿利特建材有限公司 | Hypergravity membrane reactor |
| CN114426298A (en) * | 2020-10-29 | 2022-05-03 | 中国石油化工股份有限公司 | System for carbonization method preparation aluminium hydroxide and carbonization reactor thereof |
| CN114632446A (en) * | 2022-03-01 | 2022-06-17 | 浙江长城搅拌设备股份有限公司 | High-efficiency self-suction type gas reaction stirring device |
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| CN1250746A (en) * | 1998-10-13 | 2000-04-19 | 中国石油化工集团公司 | Process for preparing artificial diasporite and gamma-alumina |
| CN2616525Y (en) * | 2003-03-10 | 2004-05-19 | 中国石油化工股份有限公司 | Reactor for preparing aluminium hydroxide |
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| CN2264173Y (en) * | 1996-06-08 | 1997-10-08 | 中国科学院山西煤炭化学研究所 | Reactor for preparing calmogastrin |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103964479A (en) * | 2013-01-28 | 2014-08-06 | 北京蓝天欣禾科技有限公司 | Nanometer aluminum hydroxide material and production process thereof |
| CN103964479B (en) * | 2013-01-28 | 2015-12-23 | 北京蓝天欣禾科技有限公司 | A kind of nano-aluminum hydroxide material and production technique thereof |
| CN104671266A (en) * | 2013-11-28 | 2015-06-03 | 北京阳光欣禾科技有限公司 | Process for preparing ultrafine aluminum hydroxide by seed crystal precipitation method |
| CN104959091A (en) * | 2015-06-08 | 2015-10-07 | 辽宁石油化工大学 | Carbonization synthesis system and application of same in preparation of pseudo-boehmite, and preparation method for pseudo-boehmite |
| CN105417560A (en) * | 2015-11-20 | 2016-03-23 | 中石化催化剂（北京）有限公司 | Method for producing pseudo-boehmite by adopting inorganic membrane reactor |
| CN105417561A (en) * | 2015-11-20 | 2016-03-23 | 中石化催化剂（北京）有限公司 | Production device and method of aluminum hydroxide |
| CN105417561B (en) * | 2015-11-20 | 2017-05-24 | 中国石油化工股份有限公司 | Production device and method of aluminum hydroxide |
| CN105417560B (en) * | 2015-11-20 | 2017-05-24 | 中国石油化工股份有限公司 | Method for producing pseudo-boehmite by adopting inorganic membrane reactor |
| CN114426298A (en) * | 2020-10-29 | 2022-05-03 | 中国石油化工股份有限公司 | System for carbonization method preparation aluminium hydroxide and carbonization reactor thereof |
| CN114426298B (en) * | 2020-10-29 | 2023-08-01 | 中国石油化工股份有限公司 | System for preparing aluminum hydroxide by carbonization method and carbonization reactor thereof |
| CN113877513A (en) * | 2021-11-15 | 2022-01-04 | 成都阿利特建材有限公司 | Hypergravity membrane reactor |
| CN114632446A (en) * | 2022-03-01 | 2022-06-17 | 浙江长城搅拌设备股份有限公司 | High-efficiency self-suction type gas reaction stirring device |
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|---|---|
| CN102838148B (en) | 2014-04-02 |
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