CN104787789B - Method for producing alumina by using coal-based solid waste - Google Patents
Method for producing alumina by using coal-based solid waste Download PDFInfo
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Abstract
A method for producing alumina by using coal-based solid waste comprises the steps of uniformly mixing crushed and finely ground fly ash or coal gangue with concentrated sulfuric acid, curing for 1-8 hours at 120-500 ℃, then carrying out reduction roasting with a reducing agent at 550-900 ℃ to obtain reduction calcine and sulfur-containing flue gas, collecting the sulfur-containing flue gas, preparing acid, returning the acid to sulfuric acid curing for cyclic use, carrying out primary leaching on the reduction calcine by using a solution containing sodium hydroxide, carrying out atmospheric desilication on primary leaching liquid by using calcium silicate slag as a desiliconization agent, then recycling, carrying out secondary leaching on primary leaching slag by using a seed mother solution to obtain a sodium aluminate crude solution, deeply desiliconizing the sodium aluminate crude solution by using lime to obtain calcium silicate slag and a sodium aluminate leaching solution, producing alumina by using the obtained sodium aluminate solution seed, and returning the ground and activated calcium silicate slag to be used as a desiliconization agent and seed crystal for the atmospheric desiliconization. The method has the advantages of simple process, low production cost, high aluminum recovery rate, good quality of aluminum oxide products, small amount of slag and the like.
Description
Technical field
The invention belongs to coal solid comprehensive utilization of waste materials, be specifically related to utilize the coal solid such as flyash, coal gangue refuse to produce the method for aluminum oxide, especially adopt soda acid process integration to produce aluminum oxide.
Background technology
Along with the fast development of modernization industry, scarcity of resources becomes one of pendulum main social problems in face of people increasingly.Produce the raw material mainly bauxite of aluminum oxide, traditional smelting process is that alkaline process produces aluminum oxide, and the silicon oxide in ore is the main harmful element during alkaline process is produced, and requires (the Al in ore of alumina silica ratio A/S in bauxite
2o
3with SiO
2mass values) be greater than 3.Alkaline process is divided into Bayer process, sintering process and integrated process, and wherein Bayer process is suitable for process containing Al
2o
3high, SiO
2low rich ore, general requirement Al
2o
3> 65%, A/S > 7, the aluminum oxide of more than 90% is produced by Bayer process in the world; It is the raw material of 3 ~ 5 that sintering process is applicable to process A/S; It is the raw material of 5 ~ 7 that integrated process is applicable to process A/S.But along with the increase of aluminium consumption, ore extraction amount increases, and bauxite resource reduces year by year, and ore aluminium grade constantly declines, and cost of winning improves constantly, and the aluminum-containing mineral of some non-bauxitic types draws attention for the production of the feasibility of aluminum oxide.
On the other hand, because coal in China production and consumption amount is huge, in the coal measures solid waste such as coal gangue, flyash that its production and consumption process output is a large amount of, disposal and the environmental problem that comprehensive utilization has become coal, power industry needs solution badly of these coal measures solid wastes.Coal gangue, flyash containing higher aluminium, are generally very important potential alumina raw materials, but due in coal gangue, flyash, and silica content can up to 40 ~ 50%, even higher, Al
2o
3with SiO
2mass values be generally less than 1, ore dressing again cannot enrichment, traditional bauxite into alumina technique cannot economic treatment, need research and development to be applicable to the Technology of coal solid waste resource feature, the flyash of research and development both at home and abroad at present extracts aluminum oxide method and is roughly divided into alkaline process and the large class of acid system two.
Alkaline process comprises direct sintering and pre-desiliconizing-sintering process etc.Direct sintering is similar to Bauxite Sintering method and produces alumina technology, comprises sintering, the master operation such as grog divides from efflorescence, leaching, carbon, calcination.Utilize the method for flyash and Wingdale combination producing aluminum oxide and cement disclosed in CN1644506A, flyash is mixed dry sintering after ore grinding by a certain percentage with limestone powder, then extract aluminum oxide with alkali stripping grog, leached mud is for the production of cement.Because direct sintering adds lime or limestone powder in a large number, a large amount of calcium silicate slag can be produced during leaching, when being raw material as adopted flyash, often produce 1 ton of aluminum oxide and will produce calcium silicate slag about 8-10 ton, if periphery does not have enough building materials market digestion capability, will certainly cause new, heap is high-volume larger and be alkaline waste discharge, forms more unmanageable solid waste environmental problem, inventory simultaneously due to high temperature sintering is large, causes sintering energy consumption high.
Carry out the process of alkali leaching pre-desiliconizing to raw material and can reduce sinter doses, thus reduce sintering energy consumption and reduce the leaching quantity of slag, the siliceous solution that pre-desiliconizing obtains simultaneously can produce the high level such as white carbon black, wollastonite silicon product.A kind of method extracting silicon-dioxide, aluminum oxide and gallium oxide from aluminous fly-ash disclosed in CN101284668A, aluminous fly-ash and sodium hydroxide solution are carried out pressure leaching in autoclave, make the stripping of part silicon, siliceous leach liquor is for the production of white carbon black, sinter after flyash after pre-desiliconizing mixes with limestone powder, sodium carbonate solution, then leach aluminium.Adopt pre-desiliconizing technology can improve the alumina silica ratio of flyash, reduce sintering amount, thus reduce alumina producing energy consumption, and the silicon products such as by-product white carbon black, wollastonite, but for large-scale total utilization of PCA, the market sale that huge white carbon black, wollastonite product face and competitive pressure very large.
Acid system mainly comprises sulfuric acid process and hydrochloric acid method, normally by the high silicon aluminum-containing raw material after certain density sulfuric acid or hydrochloric acid and calcination for activation in heating condition agitation leach, gained solution add alkali reaction generate aluminum hydroxide precipitation, filter to obtain aluminium hydroxide.A kind of method extracting aluminum oxide from flyash disclosed in CN1792802A, its technological process to be ground to 200 ~ 400 object flyash, first calcination activation 1 ~ 1.5h at 300 ~ 760 DEG C, then at 160 ~ 300 DEG C with the sulfuric acid leaching of 60 ~ 98% concentration, the slurry filtration leached is to be separated spent acid, and spent acid returns and leaches circulation, then from filter residue, leaches aluminium with water, then through condensing crystal, drying and dehydrating, calcination, γ-Al is obtained
2o
3adopt the method, the leaching rate of recovery of aluminium can reach 85%, but the method complex process, not only needs preroasting to activate, and leaching is carried out under the condition of high temperature concentrated acid, energy consumption is high, a large amount of acid carries out inefficient cycle in system, and the material of leaching, filtration, material transfer equipment is difficult to resolve certainly, operational difficulty.CN101811711A discloses a kind of Leaching in Hydrochloric Acid that adopts by the method extracting aluminum oxide in flyash, its process at 140-160 DEG C, leaches aluminium by after flyash and mixed in hydrochloric acid, then solid-liquid separation, condensing crystal, aluminum chloride calcining obtain active just aluminum oxide, by first aluminum oxide through Bayer process process for producing aluminum oxide.Acidic process aluminum oxide is not owing to needing to add slag former, and the level of residue extracted after aluminum oxide is few, meets the requirement of minimizing comprehensive utilization Industrial Solid Waste, and can obtain higher alumina recovery rate.But because the leach liquor of acidic process output needs condensing crystal, and it is higher containing crystal water to obtain aluminium intermediate product, and follow-up dehydration energy is high, causes the total energy consumption of acid oxidation aluminium high.Simultaneously due to the leaching poor selectivity of acidic process, a large amount of strippings of impurity such as iron, calcium, magnesium, titanium, the aluminium purity salt of condensing crystal output is not high, the further Bayer process process of follow-up need.
To sum up, although alkali process alumina product quality is good, and close with traditional bauxite into alumina technique, be easy to technique and realize, but the sale of by-product silicon product, the highly energy-consuming of sintering process and final calcium silicate slag quantity discharged be large etc., and problem seriously constrains alkaline process industrial application.Although acid technological process achieves minimizing and utilizes coal measures solid waste, the aluminium salt-pepper noise of traditional acid system and dehydration energy is high, aluminium poor product quality.
Summary of the invention
The object of the invention is the deficiency in order to overcome in existing coal solid refuse production aluminum oxide technology, a kind of soda acid process integration that adopts is provided to produce the method for aluminum oxide from the coal solid such as flyash, coal gangue refuse, object is by soda acid process integration, solve and utilize aluminium salt condensing crystal in coal solid refuse acidity extraction alumina technology and the problem that pyrolysis energy consumption is high, alumina product purity is low, avoid in alkalinity extraction alumina technology the defects such as sinter doses is large, energy consumption is high, the leaching quantity of slag is large simultaneously.
For achieving the above object, technical scheme of the present invention is as follows.
Utilize coal solid refuse to produce the method for aluminum oxide, comprise the steps:
(1) by the flyash of broken, fine grinding or coal gangue and the even post curing of vitriol oil mix, sulfuric acid slaking material is obtained;
(2) by the reducing roasting together with reductive agent of sulfuric acid slaking material, obtain reduced calcine and sulfur-containing smoke gas, the rear relieving haperacidity of sulfur-containing smoke gas collection returns step (1) sulfuric acid slaking and recycles;
(3) solution of reduced calcine containing sodium hydroxide once leaches, and solid-liquid separation obtains a leach liquor and a leached mud;
Return step (3) after (4) one times leach liquor carries out atmospheric silicon removing to recycle, one time leached mud seed precipitation solution carries out secondary leaching, obtains Silicon-rich slag and crude liquor of sodium aluminate;
(5) crude liquor of sodium aluminate lime deep desilication obtains calcium silicate slag and sodium aluminate solution, the sodium aluminate solution that obtained adopts carbon to divide or plants division technique production aluminum oxide, and calcium silicate slag returns step (4) as the desiliconization agent of a leach liquor atmospheric silicon removing and crystal seed.
The method utilizing coal solid refuse to produce aluminum oxide of the present invention, step (1) curing temperature is 120 ~ 500 DEG C, preferably 150 ~ 350 DEG C, curing time 1 ~ 8h.
The coal solid refuse that utilizes of the present invention produces the method for aluminum oxide, and in step (1) when flyash or coal gangue and vitriol oil mix, the vitriol oil presses H
2sO
4with Al in flyash or coal gangue
2o
3mole ratio 3:1 ~ 4:1 adds, mass concentration>=85% of the vitriol oil.
The coal solid refuse that utilizes of the present invention produces the method for aluminum oxide, and reductive agent described in step (2) is one in coal dust, colliery powder or its mixture, reducing roasting temperature 550 ~ 900 DEG C, reducing roasting time 0.1 ~ 60min.Preferred reducing roasting temperature 650 ~ 800 DEG C, reducing roasting time 0.1 ~ 15min.
The method utilizing coal solid refuse to produce aluminum oxide of the present invention, the extract technology condition of the reduced calcine described in step (3) is: Crater corrosion (molecular ratio of sodium oxide and aluminum oxide) α
k>=5, naoh concentration 50 ~ 100g/L, extraction temperature 30 ~ 100 DEG C, extraction time 30 ~ 120min.
The method utilizing coal solid refuse to produce aluminum oxide of the present invention, secondary extract technology condition described in step (4) is: extraction temperature 80 ~ 280 DEG C, batching Crater corrosion (leaching the molecular ratio of sodium oxide and aluminum oxide in rear expection solution) α
k0.8 ~ 2.0, naoh concentration 100 ~ 300g/L, extraction time 30 ~ 120min, lime-crushed stone pile 0 ~ 15%.
The method utilizing coal solid refuse to produce aluminum oxide of the present invention, a leach liquor described in step (4) carries out atmospheric silicon removing, be utilize the calcium silicate slag of step (5) crude liquor of sodium aluminate deep desilication gained as desiliconization agent and crystal seed, at 80 ~ 100 DEG C, react 30 ~ 240min; For improving the reactive behavior of calcium silicate slag, calcium silicate slag uses after grinding activation.
Sulfation slaking described in the present invention, be utilize the pyroreaction of the vitriol oil active, the aluminium of the aluminosilicate form in flyash, coal gangue changed into generation Tai-Ace S 150, reacts as shown in the formula (1), thus the mineral structure in destruction raw material, aluminium mineral and silicon mine are dissociated.
Al
2O
3·nSiO
2+3H
2SO
4＝Al
2(SO
4)
3+nSiO
2+3H
2O(1)
Reducing roasting described in the present invention, that sulfuric acid slaking material is directly carried out reducing roasting with reductive agent, the condensing crystal Tai-Ace S 150 and the crystalline sulfuric acid aluminium that avoid highly energy-consuming in acidic process aluminium oxide extraction process dewater and Roasting Decomposition operation, simultaneously, because adopting quick medium temperature roast, in calcining, the leaching activity of aluminum oxide is high, utilizes the reaction of coal reduction roasting such as formula (2).
Al
2(SO
4)
3+3/2C＝Al
2O
3+3SO
2(g)+3/2CO
2(g)(2)
In the present invention, the calcining sodium hydroxide solution that described reducing roasting obtains leaches aluminium, and Leaching reaction is as shown in the formula (3).
Al
2O
3+3H
2O+2NaOH＝2NaAl(OH)
4(3)
In order to remove the activated silica in calcining, reduced calcine first leaches desiliconization with the sodium hydroxide solution of lower concentration, and the siliceous leach liquor recycle silicon calcium slag obtained does heavy silicea and crystal seed, thus to solve in calcining the amount of activated silicon of little residue to the impact of alumina producing.
The present invention utilizes vitriol oil pyroreaction to enhance the decomposition of aluminium silicate mineral in flyash, coal gangue, different from traditional acid system, directly do not carry out the leaching of Tai-Ace S 150, but the desulfurization utilizing reductive agent to realize sulfuric acid slaking material is decomposed, and ensureing the activity of aluminum oxide, the flue gas that desulfurization produces realizes the regeneration of main agents sulfuric acid by relieving haperacidity.Method provided by the invention, leaches a difficult problem for poor selectivity, solution purification difficulty, without the need to highly energy-consuming processes such as the condensing crystal Tai-Ace S 150 in traditional sulfuric acid process, Tai-Ace S 150 dehydrations when solving traditional acidic process.Compared with traditional alkaline process treated coal ash technique, avoid the sintering circuit of highly energy-consuming, without the need to adding the slag former such as limestone powder, lime, leaching the quantity of slag and significantly reducing.
Accompanying drawing explanation
Accompanying drawing is the principle flow chart of method of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention made and further illustrating.
By the flyash of broken, fine grinding or coal gangue even with vitriol oil mix after under 120 ~ 500 DEG C of conditions slaking 1-8h, obtain sulfuric acid slaking material; Sulfuric acid slaking material is carried out reducing roasting together with reductive agent under 550 ~ 900 DEG C of temperature condition, obtains reduced calcine and sulfur-containing smoke gas, the rear relieving haperacidity of sulfur-containing smoke gas collection returns sulfuric acid slaking and recycles; The solution of reduced calcine containing sodium hydroxide once leaches, and solid-liquid separation obtains a leach liquor and a leached mud; One time leach liquor carries out the use of atmospheric silicon removing Posterior circle, and one time leached mud seed precipitation solution carries out secondary leaching, obtains Silicon-rich slag and crude liquor of sodium aluminate; Crude liquor of sodium aluminate lime deep desilication obtains calcium silicate slag and sodium aluminate solution, and the sodium aluminate solution obtained adopts carbon to divide or plants division technique produces aluminum oxide, returns the desiliconization agent as a leach liquor atmospheric silicon removing and crystal seed after calcium silicate slag grinding activation.
Be further described method of the present invention with nonlimiting examples below, to contribute to understanding content of the present invention and advantage thereof, and not as limiting the scope of the present invention, protection scope of the present invention is determined by claims.
Embodiment 1
Mixed with sulfuric acid by aluminous fly-ash that is salic 48%, silicon-dioxide 42%, sulphuric acid is Al in described flyash
2o
33.5 times of mole number, the h 2 so 4 concentration of use is 90%, after mixing, and curing temperature 250 DEG C, obtains sulfuric acid slaking material under curing time 2h condition.Sulfuric acid slaking material mixes with coal dust, and coal dust add-on is 8% of slaking material quality, carries out fast restore roasting, roasting time 5min temperature 750 DEG C.Reduced calcine once leaches, leaching condition: use Crater corrosion α
k8, the solution of naoh concentration 50g/L leaches 30min under 50 DEG C of conditions; A leached mud of gained carries out secondary leaching, leaching condition: extraction temperature 100 DEG C, Crater corrosion α
k2, naoh concentration 100g/L, extraction time 60min, the leaching yield 89% of aluminium, secondary leach liquor silica concentration 0.2g/L, obtain sodium aluminate solution and the calcium silicate slag of silica concentration 0.05g/L after the desiliconization of secondary leach liquor lime, gained sodium aluminate solution prepares aluminum oxide through kind of a division technique.
Embodiment 2
Mixed with sulfuric acid by aluminous fly-ash that is salic 48%, silicon-dioxide 42%, sulphuric acid is Al in described flyash
2o
33.5 times of mole number, the sulfuric acid concentration of use is 93%, after mixing, and curing temperature 250 DEG C, obtains sulfuric acid slaking material under curing time 2h condition.Sulfuric acid slaking material mixes with coal dust, and coal dust add-on is 8% of slaking material quality, carries out fast restore roasting, roasting time 5min temperature 750 DEG C.Reduced calcine once leaches, leaching condition: use Crater corrosion α
k8, the solution of naoh concentration 100g/L leaches 30min under 50 DEG C of conditions.The leach liquor obtained is containing silica 1 g/L, by after the calcium silicate slag fine grinding of embodiment 1 gained with this leach liquor hybrid reaction desiliconization, desilication reaction temperature 90 DEG C, time 60min, after obtaining the desiliconization containing silicon-dioxide 0.1g/L, liquid returns once to leach and recycles.A leached mud of gained carries out secondary leaching, leaching condition: extraction temperature 270 DEG C, Crater corrosion α
k2, naoh concentration 230g/L, extraction time 60min, the leaching yield 85% of aluminium, secondary leach liquor silica concentration 0.25g/L, obtain sodium aluminate solution and the calcium silicate slag of silica concentration 0.05g/L after the desiliconization of secondary leach liquor lime, gained sodium aluminate solution prepares aluminum oxide through kind of a division technique.
Embodiment 3
Mix with sulfuric acid after coal gangue that is salic 38%, silicon-dioxide 48% is ground to 0.1mm, sulphuric acid is Al in described flyash
2o
33.5 times of mole number, the sulfuric acid concentration of use is 93%, after mixing, and curing temperature 250 DEG C, obtains sulfuric acid slaking material under curing time 2h condition.Sulfuric acid slaking material mixes with coal dust, and coal dust add-on is 3% of slaking material quality, carries out fast restore roasting, roasting time 5min temperature 750 DEG C.Reduced calcine once leaches, leaching condition: use Crater corrosion α
k8, the solution of naoh concentration 100g/L leaches 30min under 50 DEG C of conditions.The leach liquor obtained is containing silicon-dioxide 5g/L, by after the calcium silicate slag fine grinding of embodiment 2 gained with this leach liquor hybrid reaction desiliconization, desilication reaction temperature 90 DEG C, time 60min, after obtaining the desiliconization containing silicon-dioxide 0.1g/L, liquid returns once to leach and recycles.A leached mud of gained carries out secondary leaching, leaching condition: extraction temperature 270 DEG C, Crater corrosion α
k2, naoh concentration 230g/L, extraction time 60min.The leaching yield 80% of aluminium, secondary leach liquor silica concentration 0.25g/L, obtain sodium aluminate solution and the calcium silicate slag of silica concentration 0.05g/L after the desiliconization of secondary leach liquor lime, gained sodium aluminate solution prepares aluminum oxide through kind of a division technique.
Embodiment 4
Mixed with sulfuric acid by aluminous fly-ash that is salic 48%, silicon-dioxide 42%, sulphuric acid is Al in described flyash
2o
34 times of mole number, the sulfuric acid concentration of use is 93%, after mixing, and curing temperature 200 DEG C, obtains sulfuric acid slaking material under curing time 2h condition.Sulfuric acid slaking material mixes with coal dust, and coal dust add-on is 8% of slaking material quality, carries out fast restore roasting, roasting time 5min temperature 800 DEG C.Reduced calcine once leaches, leaching condition: under 50 DEG C of conditions, leach 30min with the solution of Crater corrosion α k8, naoh concentration 50g/L.The leach liquor obtained is containing silicon-dioxide 0.5g/L, by after the calcium silicate slag fine grinding of embodiment 3 gained with this leach liquor hybrid reaction desiliconization, desilication reaction temperature 90 DEG C, time 60min, after obtaining the desiliconization containing silicon-dioxide 0.1g/L, liquid returns once to leach and recycles.A leached mud of gained carries out secondary leaching, leaching condition: extraction temperature 270 DEG C, Crater corrosion α
k2, naoh concentration 230g/L, lime-crushed stone pile is 5% of a leached mud quality, extraction time 60min, the leaching yield 85% of aluminium, secondary leach liquor silica concentration 0.15g/L, obtain sodium aluminate solution and the calcium silicate slag of silica concentration 0.03g/L after the desiliconization of secondary leach liquor lime, gained sodium aluminate solution prepares aluminum oxide through kind of a division technique.
Embodiment 5
Mixed with sulfuric acid by aluminous fly-ash that is salic 48%, silicon-dioxide 42%, sulphuric acid is Al in described flyash
2o
34 times of mole number, the sulfuric acid concentration of use is 93%, after mixing, and curing temperature 300 DEG C, obtains sulfuric acid slaking material under curing time 2h condition.Sulfuric acid slaking material mixes with coal dust, and coal dust add-on is 8% of slaking material quality, carries out fast restore roasting, roasting time 10min temperature 750 DEG C.Reduced calcine once leaches, leaching condition: use Crater corrosion α
k15, the solution of naoh concentration 50g/L leaches 30min under 50 DEG C of conditions.The leach liquor obtained is containing silica 1 g/L, by after the calcium silicate slag fine grinding of embodiment 3 gained with this leach liquor hybrid reaction desiliconization, desilication reaction temperature 90 DEG C, time 60min, after obtaining the desiliconization containing silicon-dioxide 0.1g/L, liquid returns once to leach and recycles.A leached mud of gained carries out secondary leaching, leaching condition: extraction temperature 100 DEG C, Crater corrosion α
k2, naoh concentration 200g/L, extraction time 60min, the leaching yield 83% of aluminium, secondary leach liquor silica concentration 0.15g/L, obtain sodium aluminate solution and the calcium silicate slag of silica concentration 0.03g/L after the desiliconization of secondary leach liquor lime, gained sodium aluminate solution prepares aluminum oxide through kind of a division technique.
Claims (9)
1. utilize coal solid refuse to produce the method for aluminum oxide, it is characterized in that, comprise the following steps:
(1) by the flyash of broken, fine grinding or coal gangue and the even post curing of vitriol oil mix, sulfuric acid slaking material is obtained;
(2) by the reducing roasting together with reductive agent of sulfuric acid slaking material, obtain reduced calcine and sulfur-containing smoke gas, the rear relieving haperacidity of sulfur-containing smoke gas collection returns step (1) sulfuric acid slaking and recycles;
(3) solution of reduced calcine containing sodium hydroxide once leaches, and solid-liquid separation obtains a leach liquor and a leached mud;
Return step (3) after (4) one times leach liquor carries out atmospheric silicon removing to recycle, one time leached mud seed precipitation solution carries out secondary leaching, obtains Silicon-rich slag and crude liquor of sodium aluminate;
(5) crude liquor of sodium aluminate lime deep desilication obtains calcium silicate slag and sodium aluminate solution, the sodium aluminate solution that obtained adopts carbon to divide or plants division technique production aluminum oxide, and calcium silicate slag returns step (4) as the desiliconization agent of a leach liquor atmospheric silicon removing and crystal seed.
2. method according to claim 1, is characterized in that, step (1) curing temperature is 120 ~ 500 DEG C, curing time 1 ~ 8h.
3. method according to claim 2, is characterized in that, step (1) curing temperature is 150 ~ 350 DEG C.
4. method according to claim 1 and 2, is characterized in that, in step (1) when flyash or coal gangue and vitriol oil mix, the vitriol oil presses H
2sO
4with Al in flyash or coal gangue
2o
3mole ratio 3:1 ~ 4:1 adds, mass concentration>=85% of the vitriol oil.
5. method according to claim 1 and 2, is characterized in that, reductive agent described in step (2) is one in coal dust, colliery powder or its mixture, reducing roasting temperature 550 ~ 900 DEG C, reducing roasting time 0.1 ~ 60min.
6. method according to claim 5, is characterized in that, reducing roasting temperature 650 ~ 800 DEG C, reducing roasting time 0.1 ~ 15min.
7. method according to claim 1 and 2, is characterized in that, the extract technology condition of the reduced calcine described in step (3) is: Crater corrosion α
k>=5, naoh concentration 50 ~ 100g/L, extraction temperature 30 ~ 100 DEG C, extraction time 30 ~ 120min.
8. method according to claim 1 and 2, is characterized in that, the secondary extract technology condition described in step (4) is: extraction temperature 80 ~ 280 DEG C, batching Crater corrosion α
k0.8 ~ 2.0, naoh concentration 100 ~ 300g/L, extraction time 30 ~ 120min, can lime be added during leaching, lime-crushed stone pile 0 ~ 15%.
9. method according to claim 1 and 2, it is characterized in that, a leach liquor described in step (4) carries out atmospheric silicon removing, be utilize the calcium silicate slag of step (5) crude liquor of sodium aluminate deep desilication gained as desiliconization agent and crystal seed, at 80 ~ 100 DEG C, react 30 ~ 240min; For improving the reactive behavior of calcium silicate slag, calcium silicate slag uses after grinding activation.
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| CN102417197A (en) * | 2010-09-28 | 2012-04-18 | 沈阳铝镁设计研究院有限公司 | Method for producing sandy alumina by fly ash |
| CN103693665A (en) * | 2012-12-28 | 2014-04-02 | 中国神华能源股份有限公司 | Method for preparing high-purity aluminum oxide from fly ash |
| CN104211094A (en) * | 2013-06-04 | 2014-12-17 | 北京矿冶研究总院 | Novel process for producing potassium carbonate, sodium carbonate and aluminum oxide by using potash feldspar ore |
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