CN113061733A - Method for preparing aluminum-rich leaching solution by using fly ash sintering activation-acid leaching method - Google Patents

Method for preparing aluminum-rich leaching solution by using fly ash sintering activation-acid leaching method Download PDF

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CN113061733A
CN113061733A CN202110295357.7A CN202110295357A CN113061733A CN 113061733 A CN113061733 A CN 113061733A CN 202110295357 A CN202110295357 A CN 202110295357A CN 113061733 A CN113061733 A CN 113061733A
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fly ash
sintering
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张梦露
李爱民
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Dalian University of Technology
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    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
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    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
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Abstract

A method for preparing an aluminum-rich leaching solution by a fly ash sintering activation-acid leaching method belongs to the field of fly ash comprehensive utilization. The method comprises the following steps: (1) ball milling the fly ash, screening and taking the fly ash with the particle size of less than 200 meshes for later use; (2) mixing the fly ash and sodium hydroxide, and performing ball milling; (3) putting the ball-milled mixture into an incinerator, and sintering under a set temperature condition; (4) configuration H in pickling bath2SO4Solution, with a liquid-solid ratio of 20: 1, adding a sintering product, and staying for 2 hours at the temperature of 80 ℃; (5) inputting the system after acid leaching into a filter for solid-liquid separation, collecting the leached acid liquor, testing the concentration of aluminum ions, and calculating leaching efficiency; (6) collecting the filter cake, placing the filter cake in a washing tank, washing with water, filtering and finally carrying out comprehensive utilization. The method for leaching aluminum from the sintering activated fly ash has the advantages of simple process and no technical requirementsHigh leaching efficiency, low sintering cost and other advantages.

Description

Method for preparing aluminum-rich leaching solution by using fly ash sintering activation-acid leaching method
Technical Field
The invention belongs to the field of comprehensive utilization of fly ash, and particularly relates to a method for leaching aluminum from sintered activated fly ash.
Background
With the continuous development of China, the energy demand is huge, and China has the current situations of rich coal, poor oil and low gas energy, so that coal is still used as a main energy source. Fly ash produced by coal-fired power plants becomes the largest single pollution source of industrial solid wastes.
Aluminum is an important metal element in industry, and aluminum and its alloys have excellent properties. Compared with bauxite, the content of alumina in the fly ash is lower, but the fly ash is suitable for large-scale comprehensive utilization and valuable element extraction due to the larger yield and more concentrated production.
Netherlands researchers Grzymek et al proposed techniques for recovering aluminum from fly ash, which successfully extracted aluminum from sintered fly ash containing more than 30% of aluminum oxide, and also used the aluminum-extracted waste residue to prepare cement. The research on aluminum extraction of fly ash in China is relatively late. From the 80 s of the 20 th century, on the basis of the experience of extracting aluminum from low-grade bauxite by reference, China continuously explores a new technology for extracting aluminum oxide by using fly ash, and the main methods comprise sintering, acid leaching, alkali leaching and the like.
1. Sintering process
The sintering method is divided into lime sintering method, soda lime sintering method, sodium carbonate sintering method, ammonium sulfate salt sintering method, fluoride sintering method and the like according to sintering media, the principle is that the structure of mullite in the fly ash is destroyed in the sintering process to form salt substances which are easy to dissolve in acid, and the alumina can be obtained through acid leaching, impurity removal, carbonization, calcination and the like. For lime and soda lime sintering methods, fly ash and lime are generally mixed and sintered at a temperature of more than 1300 ℃ to generate soluble calcium aluminate and insoluble dicalcium silicate so as to achieve the purpose of silicon-aluminum separation, but the lime sintering method has high sintering temperature, high energy consumption, large waste residue yield and easy occurrence of secondary pollution of waste residue. In recent years, sodium carbonate has been used as a sintering aid in large quantities, and the sintering temperature is relatively low, generally 850 ℃ or higher, when sodium carbonate is used for sintering as compared with the lime sintering method. Wang et al [ WANG R C, C ZHAI Y, WU X W, NING Z P, MA P H.extraction of aluminum from flash by ammonium sulfate manufacturing technology [ J ] transformations of non-ferrous Metals Society of China,2014,24(05): 1596-.
2. Acid leaching process
The acid leaching method is to use higher strong acid such as sulfuric acid or hydrochloric acid to destroy the mullite structure in the fly ash so as to realize the separation of silicon and aluminum. However, even if the strong acid is directly used for leaching, the structure of the mullite mineral phase is difficult to destroy, so more aluminum is extracted under the premise of adding a leaching aid, pressurizing and the like. After the ammonium fluoride is added in the leaching process, the extraction rate of the alumina is greatly improved, but toxic hydrogen fluoride gas is generated in the leaching process. For pressure acid leaching, although the leaching efficiency is higher than that of a pure acid leaching process, and the leaching process is clean, the process has high requirements on equipment, and the leaching cost is relatively high. The ammonium bisulfate leaching method is the same as the direct acid method, the flow is simple, the energy consumption is low, the tailing output is low, and the leaching medium can be recycled. The acidity of ammonium bisulfate is far lower than that of strong acid, the requirement on equipment is not high, but the recovery rate of alumina is limited to a certain extent, and the biggest problem of the process is that the evaporation, concentration and crystallization of an ammonium aluminum sulfate solution are difficult. Lei Shi and the like [ Lei Shi, Wuyu Sheng, ammonium bisulfate solution method for treating fly ash to produce metallurgical-grade aluminum oxide industrial feasibility analysis [ J ] light metal, 2015,10):10-13 ] research is carried out by leaching ammonium bisulfate for 3h at the temperature of 130-. However, the aluminum ammonium sulfate solution is difficult to evaporate, concentrate and crystallize, and the product purification and crystallization process is complex, so that the research on crystallization of aluminum ammonium sulfate dodecahydrate is not abundant, and most experimental exploration stays in the preparation stage of the leachate.
3. Hydrothermal alkaline process
The hydrothermal alkali method is to separate silicon and aluminum in the fly ash by using strong alkali solution such as sodium hydroxide and the like at a certain temperature. The alkaline leaching mainly comprises a two-step alkaline leaching method and a sub-molten salt method. The two-step alkaline leaching method utilizes the alkaline concentration difference of leached Si and Al to pre-desiliconize under the condition of lower alkaline concentration and recover aluminum under the condition of higher concentration. In the alkaline leaching process, the alkali concentration is too high, the circulating amount of NaOH is large, the equipment corrosion is serious, the requirement is high, the alkali consumption is extremely large, the product has strong alkalinity, and the final treatment process is complex and the cost is high. Liu Chun Li, high alumina fly ash aluminium-silicon separation application basic research [ D ]; 2019 ] the research on the synergistic dissolution mechanism of the high-alumina fly ash and the red mud and the thermodynamics of the reaction of the high-alumina fly ash sub-molten salt is carried out by taking a sodium hydroxide sub-molten salt medium as a dissolution agent, wherein the initial causticity ratio is 25, the liquid-solid ratio is 5, the concentration of sodium oxide is 370g/L, mullite is completely decomposed at 180 ℃, and corundum is completely decomposed at 220 ℃. The process of the sub-molten salt method is complex, the alkali requirement at the initial stage is large, the requirement on equipment is high, the formula of the leaching agent in the process is greatly influenced by the quality of the fly ash, the temperature control is strict, and the technical requirement is high; when the amount of aluminum left in the silicon slag is high, the alkali is difficult to recover, so that the process cannot realize circulation.
Disclosure of Invention
The invention aims to provide a method for preparing an aluminum-rich leaching solution by a fly ash sintering activation-acid leaching method, and provides an aluminum leaching method with high leaching efficiency, low sintering temperature and short sintering time.
In order to realize the purpose, the invention adopts the following technical scheme:
a method for preparing an aluminum-rich leaching solution by a fly ash sintering activation-acid leaching method comprises the following steps:
step (1), ball milling the fly ash, screening and taking the fly ash with the particle size of less than 200 meshes for later use;
step (2), mixing the fly ash obtained in the step (1) with sodium hydroxide, and carrying out ball milling;
step (3), placing the ball-milled mixture obtained in the step (2) into an incinerator, and sintering at a set temperature;
step (4), preparing H in a pickling bath2SO4Solution, with a liquid-solid ratio of 20: 1, adding the sintering product obtained in the step (3), and staying for 2 hours at the temperature of 80 ℃;
step (5), inputting the system subjected to acid leaching in the step (4) into a filter for solid-liquid separation, collecting the leached acid liquor, testing the concentration of aluminum ions, and calculating leaching efficiency;
and (6) collecting the filter cake, placing the filter cake in a water washing tank, washing with water, filtering and finally performing comprehensive utilization.
According to the method of the invention, preferably, the mass ratio of the sodium hydroxide to the fly ash in the step (2) is 0.8-1.4: 1; the mixing and ball milling time is 30-60 min.
According to the method of the present invention, preferably, the sintering temperature in step (3) is 500-700 ℃; the temperature rise rate of the incinerator before sintering is 10 ℃ min-1(ii) a The sintering time (sintering time measured from the end of the temperature raising program) is 120min or less.
According to the process of the present invention, preferably, H in step (4)2SO4The mass concentration of the solution is 20-40%.
The invention is further explained below:
1. sintering activation process
Sintering activation is a method for activating the fly ash under the high-temperature condition by using hydroxide of alkali metal or alkaline earth metal as a sintering aid. As for pulverized coal furnace fly ash, quartz, mullite and amorphous phase are tightly wrapped, and Al mainly exists in mullite and glass phase. Mullite is a crystalline structure which is compact and relatively stable and not easily damaged by linking four aluminum atoms around a silicon-oxygen tetrahedron, and a glass body is mainly divided into an aluminosilicate amorphous body formed by linking two or three aluminum atoms by the silicon-oxygen tetrahedron and a silica amorphous body formed by linking four silicon atoms by the silicon-oxygen tetrahedron. The mullite structure is stable, but can be damaged by alkali or alkaline earth compounds with larger ionic radius due to the unbalanced electrovalence of oxygen in the structure; the amorphous silicon dioxide has high activity and is easy to damage; the amorphous activity of the aluminosilicate is low, and the Si-O-Al structure can be destroyed after activation. Therefore, the invention uses sodium hydroxide as a sintering activator to excite the activity of the fly ash, so that an aluminum-containing substance is converted into an aluminum salt capable of dissolving aluminum. The main chemical reactions are:
3Al2O3·2SiO2+NaOH→xNa2O·yAl2O3·zSiO2+CO2
Al2O3+2NaOH→2NaAlO2+H2O
SiO2+2NaOH→Na2SiO3+H2O
wherein xNa as described above2O·yAl2O3·zSiO2Is aluminosilicate and presents nepheline and faujasite mineral phases in the sintered product.
2. Aluminum leaching process
The sulfuric acid can chemically react with nepheline and faujasite in the sintered product to enable aluminum to exist in an acid solution in an ion form, and effective silicon-aluminum separation can be realized. On the premise of ensuring the solubility of the aluminum sulfate in the sulfuric acid and the leaching efficiency, the concentration of the sulfuric acid is reduced as much as possible, the cost can be saved, and the equipment requirement can be reduced. The main chemical reactions are:
xNa2O·yAl2O3·zSiO2+H2SO4→Al2(SO4)3+Na2SO4+H2SiO3
Na2SiO3+H2SO4→Na2SO4+H2SiO3
compared with the prior art, the method for leaching aluminum from the sintering activated fly ash provided by the invention has the following advantages:
1. the invention utilizes the sintering activation-acid leaching process, has simpler flow and lower technical requirement, and can keep higher leaching efficiency;
2. the invention takes NaOH as a sintering activator, greatly reduces the sintering temperature, shortens the sintering time and reduces the energy consumption to a certain extent.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
Detailed Description
The following examples are intended to illustrate the invention, but not to limit it.
The following examples are intended to illustrate the invention, but not to limit it.
Example one
(1) Ball-milling the fly ash for a certain time, and then screening the fly ash to obtain a product with the particle size of less than 200 meshes;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) of 0.8;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 ℃ and sintering for 2h at 550 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 37.35%.
TABLE 1 fly ash chemical composition of certain power plant
Figure BDA0002984132150000061
Example two
(1) Ball-milling the fly ash for a certain time, and then screening the fly ash to obtain a product with the particle size of less than 200 meshes;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) 1.2;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 ℃, and sintering for 2h at 550 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 75.48%.
Example three
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 ℃, and sintering for 2h at 550 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 95.11%.
Example four
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 45min according to NaOH/CFA (wt./wt.) 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 ℃, and sintering for 2h at 550 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 82.25%.
Example five
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 60min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 ℃, and sintering for 2h at 550 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 61.44%.
Example six
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 500 ℃, and sintering for 2h at 500 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 75.54%.
Example seven
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 600 ℃, and sintering for 2h at 600 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 81.37%.
Example eight
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 650 ℃ and burning at 650 DEG CKnot 2 h.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 83.64%.
Example nine
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 700 ℃, and sintering for 2h at 700 ℃.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 82.76%.
Example ten
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 deg.C, and maintaining at 550 deg.C for 10 min.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 95.94%.
Example eleven
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 deg.C, and maintaining at 550 deg.C for 40 min.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 94.52%.
Example twelve
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash in the step (1) with sodium hydroxide according to NaOH/CFA (wt./wt.) of 1.4 for 30 min;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 deg.C, and maintaining at 550 deg.C for 80 min.
(4) 30 percent of H is prepared in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 95.79%.
Example thirteen
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 deg.C, and maintaining at 550 deg.C for 120 min.
(4) 20 percent of H is configured in a pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 77.07%.
Example fourteen
(1) Ball-milling the fly ash, screening and taking a product with a particle size of less than 200 meshes for later use;
(2) mixing and ball-milling the fly ash and sodium hydroxide in the step (1) for 30min according to NaOH/CFA (wt./wt.) ═ 1.4 respectively;
(3) after the ball milling is finished, the mixture of (2) is put into an incinerator at the temperature of 10 ℃ for min-1Heating to 550 deg.C, and maintaining at 550 deg.C for 120 min.
(4) 40% H is configured in the pickling bath2SO4Adding the sintered product (the liquid-solid ratio is 20: 1) of the step (3) after the solution is added, and staying for 2 hours at the temperature of 80 ℃;
(5) and (3) the acid leaching system enters a filter for solid-liquid separation, the leached acid liquor is collected to test the concentration of aluminum ions, and the leaching efficiency is calculated to be 80.83%.

Claims (5)

1. The method for preparing the aluminum-rich leachate by the fly ash sintering activation-acid leaching method is characterized by comprising the following steps of:
step (1), ball milling the fly ash, screening and taking the fly ash with the particle size of less than 200 meshes for later use;
step (2), mixing the fly ash obtained in the step (1) with sodium hydroxide, and carrying out ball milling;
step (3), placing the ball-milled mixture obtained in the step (2) into an incinerator, and sintering at a set temperature;
step (4), preparing H in a pickling bath2SO4Solution, with a liquid-solid ratio of 20: 1, adding the sintering product obtained in the step (3), and staying for 2 hours at the temperature of 80 ℃;
step (5), inputting the system subjected to acid leaching in the step (4) into a filter for solid-liquid separation, collecting the leached acid liquor, testing the concentration of aluminum ions, and calculating leaching efficiency;
and (6) collecting the filter cake, placing the filter cake in a water washing tank, washing with water, filtering and finally performing comprehensive utilization.
2. The method for preparing the aluminum-rich leaching solution by the fly ash sintering activation-acid leaching method according to claim 1, wherein the mass ratio of the sodium hydroxide to the fly ash in the step (2) is 0.8-1.4: 1; the mixing and ball milling time is 30-60 min.
3. The method for preparing the aluminum-rich leaching solution by the fly ash sintering activation-acid leaching method according to claim 1 or 2, wherein the sintering temperature in the step (3) is 500-700 ℃; the temperature rise rate of the incinerator before sintering is 10 ℃ min-1(ii) a The sintering time is below 120 min.
4. The method for preparing the aluminum-rich leaching solution by the fly ash sintering activation-acid leaching method according to claim 1 or 2, wherein in the step (4), H is used2SO4The mass concentration of the solution is 20-40%.
5. The method for preparing the aluminum-rich leaching solution by the fly ash sintering activation-acid leaching method according to claim 3, wherein H in the step (4)2SO4The mass concentration of the solution is 20-40%.
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