CN101767807A - Method for extracting high-purity aluminum oxide and silica gel from beauxite - Google Patents
Method for extracting high-purity aluminum oxide and silica gel from beauxite Download PDFInfo
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- CN101767807A CN101767807A CN201010013633A CN201010013633A CN101767807A CN 101767807 A CN101767807 A CN 101767807A CN 201010013633 A CN201010013633 A CN 201010013633A CN 201010013633 A CN201010013633 A CN 201010013633A CN 101767807 A CN101767807 A CN 101767807A
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Abstract
The invention discloses a method for extracting aluminum oxide and silica gel from beauxite (aluminum bauxite). In the method, steps such as cyclic activation, leaching, recovery of carbon, sodium carbonate and water, separation of silicon from aluminum, thermal decomposition and recovery of hydrochloric acid are employed to obtain high-purity aluminum oxide; in addition, CO2 produced in the whole technological process and alkaline, acid and water used in the process of extraction can all be recovered and recycled. The method of the invention features high extraction efficiency of aluminum oxide, simple technological process, high-purity obtained silica gel and major breakthroughs in solving the technical problem that a great deal of waste residue is produced in the process of traditionally extracting aluminum bauxite and deironing is costly.
Description
Technical field
The invention belongs to the comprehensive utilization technique field of metallurgy, Chemical Manufacture, particularly a kind of method of from bauxite, extracting aluminum oxide and silica gel.
Background technology
In recent years, follow the fast-developing and domestic aluminum oxide output of China's aluminium industry to increase substantially, caused rapid increase bauxite (claiming bauxitic clay again) demand.And the reserves of certain competitive power really can be exploited and have to the present bauxite of China less than 200,000,000 tons.By existing producing capacity, China's bauxite static state can be exploited the time limit approximately only 15 years.
The A/S of domestic bauxite more than 80% is 5～8 even littler middle-low bauxite, and existing alumina producer great majority can only utilize the bauxite of alumina silica ratio greater than 7 above grades.And China's alumina silica ratio only accounts for about 30% of total reserves greater than 7 bauxite, and based on diaspore type bauxite, its stripping property difference causes the production cost height.And 1 ton of aluminum oxide of the every production of most of alumina producers needs about 2.5 tons of bauxite trihydrates, therefore, and desired raw material overwhelming majority dependence on import.
As seen, bauxite becomes the bottleneck of restriction China alumina industry development gradually, at current China bauxite resource scarcity, higher-grade bauxite reserves day by day reduce, for ore deposit grade downward trend, we should accelerate exploitation and improve low-grade bauxite and utilize technology, enlarge the bauxite available volume of resources, improve resource utilization.So, could make the alumina industry development of China no longer be subjected to world market bauxite to supply the restriction of situation.In addition, present alumina producing technology also can be discharged the waste of enormous amount---and red mud and depleted low-grade bauxite, caused resource serious waste and environmental pollution.
The invention provides a kind of production method of extracting high-purity alpha-alumina and silica gel from bauxite, to the alumina silica ratio no requirement (NR), and this working of an invention can reduce the grade of bauxite, the situation of alleviation China bauxite scarcity.This invention simultaneously to equipment in the production process require low, bed drain purge is little, cost is low.
Summary of the invention
The purpose of this invention is to provide a kind of method of from bauxite, extracting high-purity alpha-alumina and silica gel, this method to grade, alumina silica ratio and the equipment of bauxite require low, bed drain purge is little, cost is low.
To achieve these goals, the present invention takes following technical solution:
A kind of method of extracting high-purity alpha-alumina and silica gel from bauxite is characterized in that, comprises the following steps:
Step 1: get bauxite and Na
2CO
3By bauxite: yellow soda ash is 1: 0.3～1: 4 mixed, pulverizes, is milled down to 150 orders～300 orders, controlled temperature roasting under 500 ℃～1000 ℃ conditions then, and roasting time is 20 minutes～90 minutes.Calciner connects gas output tube during roasting, and is connected with carbon branch pond.
Step 2: it is 0～20% sodium hydroxide solution that the product of roasting that step 1 is obtained adds weight percent concentration, and to make the solid-liquid mass ratio be 1: 3～1: 50, and leaching temperature is 10 ℃～100 ℃, and leaching time is 5 minutes～90 minutes.The leaching after-filtration obtains filtrate and filter residue respectively.The composite mixture of filter residue and bauxite can continue embodiment and condition circulation calcination activation with step 1, and adopts the leaching of this step method condition to utilize.
Step 3:, be connected to condensing works simultaneously and reclaim distilled water with step 2 gained filtrate evaporation concentration under condition of negative pressure.Filtrate be concentrated into original volume 10%～50% after, insert in the carbon branch pond, normal pressure or pressurized conditions feed down CO
2Carry out the carbon branch.Carbon branch temperature remains on 20 ℃～100 ℃, and filtrate pH value 4～10 is divided terminal point as carbon.Carbon divides after-filtration, and filter residue is H
2SiO
3And Al (OH)
3Mixture, filtrate are Na
2CO
3Solution.
Step 4: with the Na of step 3 gained
2CO
3Crystallization of solution negative pressure evaporation and oven dry, promptly recyclable yellow soda ash.The yellow soda ash that reclaims can be directly used in the circulation calcination activation process of gained filter residue and the composite mixture of bauxite in step 1 or the step 2.Na
2CO
3In the solution heating negative pressure evaporation process, connecing condensing works and storage tank is recyclable distilled water.
Step 5: to the H of step 3 gained
2SiO
3And Al (OH)
3In the mixture, add the refining hydrochloric acid of 3mol～10mol, the solid-liquid mass ratio is 1: 1～1: 10, keeps 3 minutes～120 minutes after-filtration of reaction under 10 ℃～100 ℃ conditions of temperature, obtains AlCl respectively
3Seminal fluid and filter residue.Filter residue ageing, washing obtain pure silica gel;
Step 6: with step 5 gained AlCl
3Seminal fluid concentrates, and obtains AlCl
3Crystal.With AlCl
3Crystal places the pyrolysis installation of can discharging fume, and pyrolysis is 0.5 hour～12 hours under 260 ℃～1200 ℃ conditions, obtains high-purity aluminum oxide, reclaims hydrochloric acid simultaneously.
Utilize the present invention, not only can reduce the bauxite taste and require, solve the insufficient problem of China's higher-grade bauxite, can also make that the siliceous composition in the bauxite obtains high value added utilization, reduced the discharging wastes amount simultaneously.In addition, the CO that produces in the whole technological process
2And it is all recyclable and realize recycle to carry in the aluminium process employed alkali, acid and water.This method has the extraction yield height to aluminium and silicon, the characteristics that the process implementing difficulty is little, bed drain purge is few.Especially having broken through current bauxite, to extract deironing cost in the alumina process high and produce the difficult problem of a large amount of filter residues, not only simplified the technological process of bauxite deironing, also can effectively reduce production costs.
Description of drawings
Fig. 1 is the process flow sheet that extracts high purity aluminium oxide and silica gel from bauxite.
Fig. 2 is the recovery process flow sheet of yellow soda ash and water.
Fig. 3 is the process flow sheet of fs salt acid recovery.
Fig. 4 is the process flow sheet of subordinate phase salt acid recovery.
Embodiment
The present invention is described in further detail below in conjunction with embodiment that accompanying drawing and contriver provide.
Fig. 1 is one embodiment of the present of invention, promptly extracts the living technology journey figure of high purity aluminium oxide and silica gel from bauxite.Specifically comprise the following steps:
Step 1: make bauxite and Na
2CO
3Mix by 1: 0.3～1: 4 mass ratio, and pulverize, be milled down to 150 orders～300 orders, controlled temperature roasting under 500 ℃～1000 ℃ conditions then, roasting time is 20 minutes～90 minutes.Calciner connects gas output tube during roasting, and is connected with carbon branch pond, is convenient to make the CO that produces during the calcining
2Gas is directly used in carbon branch process.The main thing of sinter after the roasting is sodium metaaluminate, water glass mutually.
The main chemical reactions that takes place in the sintering process is as follows:
Al
2O
3+Na
2CO
3＝2NaAlO
2+CO
2↑
SiO
2+Na
2CO
3＝Na
2SiO
3+CO
2↑
Step 2: in the product of roasting that step 1 is obtained, add concentration and be 0～20% sodium hydroxide solution, and to make solid-to-liquid ratio be 1: 3～1: 50, it leached, leaching time 5 minutes～90 minutes under 10 ℃～100 ℃ temperature condition.
After the leaching, Na
2SiO
3And NaAlO
2Be dissolved in the water, filter to get filtrate and filter residue.The composite mixture of filter residue and bauxite continues mode and condition circulation calcination activation with step 1, and adopts this step method and condition leaching to utilize.
The method of circulation calcination activation is, with step 2 gained filter residue and the composite mixture of bauxite, with Na
2CO
3According to 1: 0.3～1: 4 mixed, pulverizing, levigate back roasting, 500 ℃～1000 ℃ of maturing temperatures, roasting time 20 minutes～90 minutes.
Step 3: step 2 gained filtrate is concentrated into 10%～50% of original volume, inserts in the carbon branch pond, normal pressure or pressurized conditions feed CO down
2Carry out the carbon branch.Carbon branch temperature remains on 20 ℃～100 ℃, and filtrate pH value 4～10 is divided terminal point as carbon.The chemical reaction that carbon divides process to take place is as follows:
Na
2SiO
3+CO
2+H
2O→H
2SiO
3↓+Na
2CO
3
2NaAlO
2+CO
2+3H
2O→2Al(OH)
3↓+Na
2CO
3
2NaOH+CO
2→H
2O+Na
2CO
3
Carbon divides after-filtration, and filter residue is H
2SiO
3And Al (OH)
3Mixture, filtrate are Na
2CO
3Solution.
Step 4: with the Na of step 3 gained
2CO
3Crystallization of solution negative pressure evaporation and oven dry, promptly recyclable yellow soda ash (see figure 2).The yellow soda ash that reclaims is directly used in the circulation calcination activation of gained filter residue and the composite mixture of bauxite in step 1 and the step 2.
Na
2CO
3In the solution heating negative pressure evaporation process, connecing condensing works and storage tank is recyclable distilled water (see figure 2).
Step 5: to the H of step 3 gained
2SiO
3And Al (OH)
3Mixture, the refining hydrochloric acid of adding 3mol～10mol, solid-to-liquid ratio is 1: 1～1: 10, keeps 3 minutes～120 minutes after-filtration of reaction under 10 ℃～100 ℃ conditions of temperature, obtains AlCl respectively
3Seminal fluid and filter residue.Filter residue ageing, washing obtain pure silica gel.
H
2SiO
3And Al (OH)
3The main chemical reactions that mixture adds the acid generation is as follows:
Al(OH)
3+3HCl→AlCl
3+3H
2O
Step 6: with step 5 gained AlCl
3Seminal fluid concentrates, and obtains AlCl
3Xln.With AlCl
3Crystal places the pyrolysis installation of can discharging fume, and pyrolysis is 0.5 hour～12 hours under 260 ℃～1200 ℃ conditions, obtains high-purity aluminum oxide.
The chemical reaction that pyrolysis takes place is:
AlCl
3·6H
2O→Al
2O
3+6HCl↑+3H
2O
By above step, can be with the Al more than 85% in the bauxite
2O
3Extract, simultaneously siliceous component more than 80% is extracted so that the form of silica gel is separated.
Aforesaid method also comprises the hydrochloric acid recycling step, and described salt acid recovery is divided into following two stages:
Fs is with the AlCl after the aluminium silicon separation in the step 5
3Seminal fluid heating negative pressure evaporation connects condensing works, absorption tower, reclaims hydrochloric acid, sees Fig. 3;
Subordinate phase is with AlCl in the step 6
3The hydrogen chloride gas that the crystal pyrolytic process decomposites connects condensing works and is dissolved in the dilute hydrochloric acid that water or fs reclaim, and big (hydrochloric acid of 3mol～8mol) is seen Fig. 4 thereby form concentration.
Described concentration is big, and (hydrochloric acid of 3mol～8mol) is capable of circulation to be used for the sepn process of step 5 sial.
The distilled water of the described recovery step 2 that is used for capable of circulation.
The method of described circulation calcination activation is, with the composite mixture of gained filter residue and bauxite in the step 2, with Na
2CO
3According to 1: 0.3～1: 4 mixed, pulverize, be milled down to 150 orders～300 orders, 500 ℃～1000 ℃ of maturing temperatures, 20 minutes～120 minutes calcination activation time.
Below be the embodiment that the contriver provides, need to prove that these embodiment are some more excellent examples, the invention is not restricted to these embodiment.
Embodiment 1:
1, gets bauxite and Na
2CO
3By 1: 1.2 mixed, pulverize, be milled down to 150 orders, roasting obtained product of roasting in 20 minutes under 700 ℃ of conditions of temperature.Calciner connects gas output tube during roasting, and is connected with carbon branch pond, and institute's exhaust body is directly used in carbon branch process.
2, the product of roasting that step 1 is obtained adds entry, and the solid-to-liquid ratio that makes product of roasting and water is that 1: 5, temperature are 30 minutes after-filtration of leaching under 80 ℃ of conditions, obtains filtrate and filter residue.
3, step 2 gained filtrate is concentrated into the original solution volume 20% after, feed CO
2Carry out the carbon branch.Make solution temperature remain on 60 ℃ of carbon branches in the carbon branch process, treat its pH value to 6 after-filtration, filter residue is H
2SiO
3And Al (OH)
3Mixture, filtrate are Na
2CO
3Solution.
4, the Na that step 3 is obtained
2CO
3The solution negative pressure evaporation reclaims Na
2CO
3Na
2CO
3The steam that produces in the solution negative pressure evaporation process connects the recovery of condensing works and storage tank and obtains distilled water.
5, the filter residue that step 3 is obtained, the refining hydrochloric acid of adding 3mol, reaction is 80 minutes under solid-to-liquid ratio 1: 6,90 ℃ of conditions of temperature.Filter and obtain AlCl respectively
3Seminal fluid and filter residue.Obtain pure silica gel after filter residue ageing, the washing;
6, with the AlCl of step 5 gained
3Seminal fluid is concentrated into AlCl
3Xln is separated out, and is placed in the pyrolysis installation that the acid recovery system is housed, and pyrolysis is 7 hours under 500 ℃ of conditions, obtains high purity aluminium oxide, reclaims hydrochloric acid simultaneously.
The salt acid recovery is divided into following two stages:
Fs is with the AlCl after the aluminium silicon separation in the step 5
3The seminal fluid negative pressure evaporation connects condensing works, absorption tower, is recovered to hydrochloric acid;
Subordinate phase is with AlCl in the step 6
3The hydrogen chloride gas that the crystallization pyrolytic process decomposites connects condensing works and is dissolved in the dilute hydrochloric acid that the fs reclaims, and forms the hydrochloric acid of concentration 3.0mol.
Embodiment 2:
1, the Na of step 2 gained filter residue and recovery among the embodiment 1
2CO
3By 1: 0.8 mixed, be milled down to 200 orders, stir, roasting obtained product of roasting in 20 minutes under 800 ℃ of conditions of temperature.Calciner connects gas output tube during roasting, and is connected with carbon branch pond, is directly used in carbon branch process.
2, the product of roasting adding concentration that step 1 is obtained is 5% sodium hydroxide solution (the dissolved in distilled water dilute hydrogen sodium oxide that is obtained by embodiment 1 step 4 obtains), and to make solid-to-liquid ratio be under 1: 10,50 ℃ of conditions of temperature, leach 90 minutes after-filtration, obtain filtrate and filter residue.
3, step 2 gained filtrate is concentrated into 15% of original volume, in concentrated filtrate, feeds CO
2, treat its pH value to 6 after-filtration, filter residue is H
2SiO
3And Al (OH)
3Mixture, filtrate are Na
2CO
3Solution.
4, the Na that step 3 is obtained
2CO
3The solution negative pressure evaporation reclaims Na
2CO
3Na
2CO
3The steam that produces in the solution negative pressure evaporation process connects the recovery of condensing works and storage tank and obtains distilled water.
5, the hydrochloric acid that will be among the embodiment 1 reclaims the concentration 3mol that obtains joins in the filter residue that step 3 obtains, and reaction 50 minutes under make solid-to-liquid ratio 1: 4,100 ℃ of conditions of temperature, filters and obtains AlCl respectively
3Seminal fluid and filter residue.The distilled water that filter residue utilizes embodiment 1 step 4 to obtain carries out ageing, washing, obtains pure silica gel;
6, with the AlCl of step 6 gained
3Seminal fluid is concentrated into AlCl
3Xln is separated out, and is placed in the pyrolysis installation that the acid recovery system is housed, and pyrolysis is 5 hours under 800 ℃ of conditions, obtains high purity aluminium oxide, reclaims hydrochloric acid simultaneously.
The salt acid recovery is divided into following two stages:
Fs is with the AlCl after the aluminium silicon separation in the step 5
3The seminal fluid negative pressure evaporation connects condensing works, absorption tower, reclaims hydrochloric acid;
Subordinate phase is with AlCl in the step 6
3The hydrogen chloride gas that the crystallization pyrolytic process decomposites connects condensing works and is dissolved in the dilute hydrochloric acid that the fs reclaims, and forms the hydrochloric acid of concentration 3.3mol.
Embodiment 3:
1, with the step 2 gained filter residue of bauxite, embodiment 2 and the Na of embodiment 2 recovery
2CO
3, successively by 2: 1: 2 mixed, pulverize, be milled down to 200 orders, roasting obtained product of roasting in 40 minutes under 800 ℃ of conditions of temperature.Calciner connects gas output tube during roasting, and is connected with carbon branch pond, is directly used in carbon branch process.
2, the product of roasting adding concentration that step 1 is obtained is 15% sodium hydroxide solution (the dissolved in distilled water dilute hydrogen sodium oxide that is obtained by embodiment 2 steps 4 obtains), and to make solid-to-liquid ratio be under 1: 15,60 ℃ of conditions of temperature, leach 1 hour after-filtration, obtain filtrate and filter residue.
3, step 2 gained filtrate is concentrated into 15% of original volume, in concentrated filtrate, feeds CO
2, treat its pH value to 9 after-filtration, filter residue is H
2SiO
3And Al (OH)
3Mixture, filtrate are Na
2CO
3Solution.
4, the Na that step 3 is obtained
2CO
3The solution negative pressure evaporation reclaims Na
2CO
3Na
2CO
3The steam that produces in the solution negative pressure evaporation process connects the recovery of condensing works and storage tank and obtains distilled water.
5, be the hydrochloric acid of 3.3mol with the concentration that reclaims among the embodiment 2, join in the filter residue that step 3 obtains, and reaction 60 minutes under make solid-to-liquid ratio 1: 8,100 ℃ of conditions of temperature, filter and obtain AlCl
3Seminal fluid and filter residue.The distilled water that filter residue utilizes embodiment 2 steps 4 to obtain carries out ageing, washing, obtains pure silica gel;
6, with the AlCl of step 6 gained
3Seminal fluid is concentrated into AlCl
3Xln is separated out, and is placed in the pyrolysis installation that the acid recovery system is housed, and pyrolysis is 2 hours under 1200 ℃ of conditions, obtains high purity aluminium oxide, reclaims hydrochloric acid simultaneously.
The salt acid recovery is divided into following two stages:
Fs is with the AlCl after the aluminium silicon separation in the step 5
3The seminal fluid negative pressure evaporation connects condensing works, absorption tower, reclaims hydrochloric acid;
Subordinate phase is with AlCl in the step 6
3The hydrogen chloride gas that the crystallization pyrolytic process decomposites connects condensing works and is dissolved in the dilute hydrochloric acid that the fs reclaims, and forms the hydrochloric acid of concentration 3.5mol.
The foregoing description can also be enumerated, and needs only in the parameter area of the technical scheme that the present invention provides according to experiment showed, of applicant, and those skilled in the art all can extract high-purity alpha-alumina and silica gel with reference to embodiments of the invention from bauxite.
Claims (10)
1. a method of extracting high-purity alpha-alumina and silica gel from bauxite is characterized in that, comprises the following steps:
Step 1: get bauxite and Na
2CO
3By bauxite: yellow soda ash is that 1: 0.3～1: 4 mass ratio mixes, pulverizes, is milled down to 150 orders～300 orders, controlled temperature roasting under 500 ℃～1000 ℃ conditions then, and roasting time is to obtain product of roasting in 20 minutes～90 minutes; Calciner connects gas output tube during roasting, and is connected with carbon branch pond;
Step 2: it is 0～20% sodium hydroxide solution that the product of roasting that step 1 is obtained adds weight percent concentration, and to make the solid-liquid mass ratio be 1: 3～1: 50, and leaching temperature is 10 ℃～100 ℃, and leaching time is 5 minutes～90 minutes; The leaching after-filtration obtains filtrate and filter residue respectively; The composite mixture of filter residue and bauxite continues with step 1 circulation calcination activation, and adopts step 2 leaching to utilize.
Step 3:, be connected to condensing works simultaneously and reclaim distilled water with step 2 gained filtrate evaporation concentration under condition of negative pressure; Filtrate be concentrated into original volume 10%～50% after, insert in the carbon branch pond, normal pressure or pressurized conditions feed down CO
2Carry out the carbon branch; Carbon branch temperature remains on 20 ℃～100 ℃, and filtrate pH value 4～10 is divided terminal point as carbon; Carbon divides after-filtration, and filter residue is H
2SiO
3And Al (OH)
3Mixture, filtrate are Na
2CO
3Solution;
Step 4: with the Na of step 3 gained
2CO
3Crystallization of solution negative pressure evaporation and oven dry, promptly recyclable yellow soda ash; The yellow soda ash that reclaims is directly used in the circulation calcination activation process of filter residue described in step 1 or the step 2 and the composite mixture of bauxite; Na
2CO
3In the solution heating negative pressure evaporation process, connect condensing works and storage tank and reclaim distilled water;
Step 5: to the H of step 3 gained
2SiO
3And Al (OH)
3In the mixture, add the refining hydrochloric acid of 3mol～10mol, the solid-liquid mass ratio is 1: 1～1: 10, keeps 3 minutes～120 minutes after-filtration of reaction under 10 ℃～100 ℃ conditions of temperature, obtains AlCl respectively
3Seminal fluid and filter residue; Filter residue ageing, washing obtain pure silica gel;
Step 6: with step 5 gained AlCl
3Seminal fluid concentrates, and obtains AlCl
3Crystal.With AlCl
3Crystal places the pyrolysis installation of can discharging fume, and pyrolysis is 0.5 hour～12 hours under 260 ℃～1200 ℃ conditions, obtains high-purity alpha-alumina and hydrochloric acid.
2. the method for claim 1 is characterized in that, further comprises hydrochloric acid recycling step 7, and described salt acid recovery divides following two stages:
Fs is with the AlCl after the aluminium silicon separation in the step 5
3Seminal fluid heating negative pressure evaporation connects condensing works and absorption tower simultaneously successively, reclaims hydrochloric acid;
Subordinate phase is with AlCl in the step 6
3The hydrogen chloride gas that the crystal pyrolytic process decomposites connects condensing works and is dissolved in the hydrochloric acid that water or fs reclaim, and is the hydrochloric acid of 3mol～8mol thereby form concentration; Described concentration is hydrochloric acid recycle in step 5 of 3mol～8mol.
3. the method for claim 1 is characterized in that, the recycle in step 2 of the distilled water of described recovery, and the residue washing that is used for step 5 is to obtain pure silica gel.
4. the method for claim 1 is characterized in that, the method for described circulation calcination activation is with the composite mixture of gained filter residue and bauxite in the step 2, with the condition circulation calcination activation of step 1, and to adopt the leaching of step 2 method condition to utilize; In the described mixture, the shared mass ratio of filter residue can be 0～100%;
5. the method for claim 1 is characterized in that, calciner connects gas output tube during described step 1 roasting, and is connected the CO that arranges with carbon branch pond
2Gas is directly used in the carbon branch process of step 3; It is 0～20% sodium hydroxide solution that the product of roasting that step 1 is obtained adds concentration of volume percent, and to make the solid-liquid mass ratio be 1: 3～1: 50, and leaching temperature is 10 ℃～100 ℃, and leaching time is 5 minutes～90 minutes.
6. the method for claim 1 is characterized in that, with step 2 gained filtrate be concentrated into original volume 10%～50% after, insert in the carbon branch pond, normal pressure or pressurized conditions feed down CO
2Carry out the carbon branch; Carbon branch temperature remains on 20 ℃～100 ℃, and filtrate pH value 4～10 is divided terminal point as carbon.
7. the method for claim 1 is characterized in that, with the Na of step 3 gained
2CO
3Yellow soda ash is reclaimed in crystallization of solution negative pressure evaporation and oven dry; The yellow soda ash that reclaims is directly used in the circulation calcination activation process of gained filter residue and the composite mixture of bauxite in step 1 or the step 2.
8. the method for claim 1 is characterized in that, to the H of step 3 gained
2SiO
3And Al (OH)
3Mixture adds the refining hydrochloric acid of 3mol～10mol, and to make the solid-liquid mass ratio be 1: 1～1: 10, keeps under 10 ℃～100 ℃ conditions of temperature reaction 3 minutes～120 minutes.
9. the method for claim 1 is characterized in that, the filter residue ageing of step 5 gained, washing obtain pure silica gel; Step 5 gained AlCl
3Crystal places the pyrolysis installation of can discharging fume, and pyrolysis is 0.5 hour～12 hours under 260 ℃～1200 ℃ conditions.
10. the method for claim 1 is characterized in that, with composite mixture of gained filter residue and bauxite and Na in bauxite or the step 2
2CO
3Mix, pulverize, be milled down to 150 orders～300 orders by 1: 0.3～1: 4 mass ratio, controlled temperature roasting under 500 ℃～1000 ℃ conditions then, roasting time is 20 minutes～90 minutes.
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| CN101913615A (en) * | 2010-07-20 | 2010-12-15 | 潘爱芳 | Method for improving alumina silica ratio of low-grade bauxite |
| CN102180498A (en) * | 2011-01-07 | 2011-09-14 | 潘爱芳 | Method for extracting alumina from bauxite |
| CN102180495A (en) * | 2011-01-07 | 2011-09-14 | 潘爱芳 | Method for producing aluminum oxide by using bauxite |
| CN102198956A (en) * | 2011-04-07 | 2011-09-28 | 付克明 | New process for producing aluminum and silicon chemical products by low-grade bauxite or kaolin raw material based on alkaline method |
| CN102659119A (en) * | 2012-04-18 | 2012-09-12 | 中国科学院过程工程研究所 | Method for separating and recovering silicon from high silicon acid liquid |
| CN105197973A (en) * | 2015-09-09 | 2015-12-30 | 洛阳国兴矿业科技有限公司 | Method of utilizing low-quality bauxite to prepare aluminum oxide |
| CN106032285A (en) * | 2015-03-13 | 2016-10-19 | 中国石油化工股份有限公司 | Method for recovering alumina |
| US9534274B2 (en) * | 2012-11-14 | 2017-01-03 | Orbite Technologies Inc. | Methods for purifying aluminium ions |
| WO2019086792A1 (en) | 2017-10-31 | 2019-05-09 | Ib2 | Method for processing bauxite |
| CN111072071A (en) * | 2019-12-13 | 2020-04-28 | 潘爱芳 | Method for producing polymeric aluminum ferric sulfate water purifying agent and silica gel by using iron tailings |
| CN111129632A (en) * | 2019-11-22 | 2020-05-08 | 深圳清华大学研究院 | Method for recycling anode and cathode mixed materials of waste ternary lithium ion battery |
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| US4254088A (en) * | 1979-03-27 | 1981-03-03 | The United States Of America As Represented By The United States Department Of Energy | Salt-soda sinter process for recovering aluminum from fly ash |
| IL116409A (en) * | 1995-12-15 | 1999-11-30 | Mashal Alumina Ind Ltd | Process for the recovery of alumina and silica |
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