CN111233003B - Acid-base combined process for completely realizing resource utilization of high-fluorine secondary aluminum ash - Google Patents
Acid-base combined process for completely realizing resource utilization of high-fluorine secondary aluminum ash Download PDFInfo
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Abstract
The invention provides an acid-base combined process for completely realizing resource utilization of high-fluorine secondary aluminum ash, which comprises the following steps of: ball-milling the high-fluorine secondary aluminum ash, screening to remove metallic aluminum, and dividing into two parts; one part is subjected to water leaching and acid leaching, and then solid-liquid separation is carried out to obtain acid leaching solution and acid leaching residue; mixing the other part with an alkaline solution, and performing solid-liquid separation after alkaline leaching to obtain an alkaline leaching solution and alkaline leaching residues; mixing the acid leaching solution and the alkali leaching solution in proportion, enabling the pH value to be close to neutral, stirring, filtering, drying the solid, roasting, dehydrating to obtain an electrolyte product, and returning the filtrate to the ball milling process. The method realizes the harmless utilization of the high-fluorine secondary aluminum ash, produces recyclable products such as electrolyte, ammonia water, high-purity aluminum oxide and salts, realizes resource circulation, effectively solves the problem of neutralization of a single acid process or alkali process, reduces the acid-alkali consumption of unit electrolytic aluminum ash treatment and the production of byproduct salts, improves the economic benefit of enterprises, and has important practical significance and practical value.
Description
Technical Field
The invention relates to the field of recycling of waste resources in the aluminum industry, in particular to an acid-base combined process for completely realizing resource utilization of high-fluorine secondary aluminum ash.
Background
In recent years, the aluminum industry in China develops rapidly, the yield is continuously increased, the aluminum production is a world large country, and a large amount of aluminum ash is generated in the aluminum industrial production process. The main substances in the aluminum ash are metallic aluminum, oxides, aluminum nitride, fluorides, salt solvents and the like, and the aluminum ash has high recycling value, but various substances exist in a complex mixed state, are difficult to separate and recycle, and have high cost, so that many enterprises abandon the resources and carry out stockpiling or landfill treatment on the resources. On one hand, the high-fluorine secondary aluminum ash (the rest part of the aluminum ash after aluminum extraction, the fluorine content is generally more than 5 percent) has serious environmental pollution, and fluoride contained in the high-fluorine secondary aluminum ash can be converted into HF gas under certain conditions or transferred into underground water and soil after being leached to cause serious standard exceeding of fluorine, so that the high-fluorine secondary aluminum ash has great influence on the air environment and human health, and therefore, the aluminum ash discharged by smelting non-ferrous metal aluminum is taken as toxic dangerous waste and inflammable dangerous waste in the published national hazardous waste record; on the other hand, fluorine-containing minerals in nature such as fluorite, apatite, cryolite and the like face serious shortage crisis, fluorine resources in the high-fluorine secondary aluminum ash have great recycling value, and from the viewpoint of resource circulation and sustainable development, the development of a process for extracting the fluorine resources from wastes in the fluorine industry has important economic and environmental significance.
The electrolyte is a complex mixture consisting of three elements of fluorine, sodium and aluminum, namely cryolite, various fluoride additives and alumina in a high-temperature molten state in the high-temperature aluminum electrolysis process, is one of essential substances in the aluminum electrolysis industry, and can reduce the electrolysis temperature, improve the current efficiency, reduce the energy consumption and improve the economic benefit in the aluminum electrolysis process.
At present, the treatment of the high-fluorine secondary aluminum ash comprises wet leaching and fire roasting. After the wet method usually adopts a leaching mode to remove fluorine, a large amount of acid or alkali is needed to be added for neutralization to prepare fluorine salt, but the price of the fluorine salt is low, a large amount of waste water is generated, and the economy is not high; and the fire method usually adopts an alkali sintering method, so that the process is too complex, part of fluorine element is lost, and high value-added products are not produced. In summary, a whole set of process for recycling fluorine elements in the high-fluorine secondary aluminum ash, preparing high value-added products and realizing comprehensive utilization of the aluminum ash is lacked. Patent CN110304646A discloses a method for efficiently separating fluorine, chlorine and nitrogen components from aluminum ash and co-producing alumina concentrate, the method mixes the aluminum ash with water for desalination and denitrification treatment, then carries out solid-liquid separation, and mixes the solid phase with alkali liquor for defluorination reaction and then filters and washes; and then carrying out neutralization reaction on the liquid phase by using dilute acid, adjusting the pH of the solution to be neutral, and carrying out defluorination reaction to obtain the villiaumite. The fluorine salt obtained by the method has low value and is not economical in industrial application. Patent CN109365473A discloses a method for defluorinating and recycling secondary aluminum ash by using a mixed-series method, which utilizes an alkali sintering method to treat high-fluorine secondary aluminum ash, and uses alkali liquor to absorb volatilized silicon fluoride gas to obtain sintered clinker; soaking the sintered clinker in water, adding a defluorinating agent into the leaching solution, stirring and filtering to obtain a purified solution; the defluorinated solution is then incorporated into the bayer process flow of low-fluorine secondary aluminum ash according to the caustic ratio. The method adopts roasting and then leaching, has the defects of complex process, high energy consumption, high alkali consumption and the like, and is difficult to industrially implement. Patent CN101823741A discloses a method for continuously producing aluminum electrolysis raw material high fluorine alumina, cryolite and water glass by using aluminum ash, firstly adding water into the aluminum ash for soaking, filtering, evaporating filtrate to obtain NaCl and KCl mixed crystals; roasting the filter residue at high temperature; then adding HF solution into the roasted product, stirring, carrying out soaking reaction, and filtering; drying the solid obtained after evaporating and concentrating the filtrate, and then producing cryolite evaporation mother liquor according to the prior art to react with NaOH; drying the filter residue at 90-110 deg.C for 12In hours, MgF is obtained2High fluorine alumina. The method has the advantages of complex process, high energy consumption, low product value and low economy. Therefore, it is necessary to provide a method for utilizing secondary aluminum ash resources, which can fully utilize secondary aluminum ash resources, reduce pollution, and is low in cost and simple and convenient to operate.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides an acid-alkali combination process for completely realizing resource utilization of high-fluorine secondary aluminum ash, and aims to comprehensively recover secondary aluminum ash resources, reduce environmental pollution, effectively solve the problem of neutralization of a single acid process or alkali process, reduce the acid-alkali consumption of unit electrolytic aluminum ash treatment, reduce byproduct salt output, greatly reduce production cost and obviously improve the economic benefit of enterprises.
In order to achieve the purpose of the invention, the invention adopts the following technical scheme: an acid-base combined process for completely realizing resource utilization of high-fluorine secondary aluminum ash comprises the following steps:
(1) ball-milling the high-fluorine secondary aluminum ash, screening to remove metallic aluminum, and dividing into A, B parts of aluminum ash;
(2) mixing A part of aluminum ash with water, heating, stirring and leaching;
(3) mixing the slurry leached in the step (2) with acid, and stirring and leaching at normal temperature;
(4) carrying out solid-liquid separation on the slurry subjected to acid leaching in the step (3) to obtain acid leaching solution and acid leaching residue;
(5) directly mixing B part of aluminum ash with an alkali solution, heating, stirring and leaching;
(6) carrying out solid-liquid separation on the slurry obtained after the alkaline leaching in the step (5) to obtain an alkaline leaching solution and alkaline leaching residues;
(7) mixing the acid leaching solution obtained in the step (4) and the alkali leaching solution obtained in the step (6) in proportion, and then adjusting the pH value to 5-8;
(8) heating and stirring the mixed solution obtained in the step (7), and carrying out solid-liquid separation to obtain electrolyte and residual liquid;
(9) washing, drying and roasting the electrolyte obtained in the step (8) to obtain an electrolyte product;
(10) and (4) returning the residual liquid obtained in the step (8) to the ball milling process in the step (1) to realize circulation.
Preferably, the sieve used for sieving in the step (1) has a pore size of 0.074 mm.
Preferably, the water immersion temperature in the step (2) is 90-100 ℃, the water immersion time is 4-6h, and the liquid-solid ratio of water to aluminum ash is (4-6): 1-2.
Preferably, the steps (2) and (5) further comprise recovering ammonia gas generated in the water leaching/alkaline leaching process and preparing the ammonia gas into ammonia water.
Preferably, H is obtained after the slurry is mixed with acid in the acid leaching in the step (3)+The concentration is 2-4mol/L, the liquid-solid ratio of the slurry after acid leaching is (5-10) to 1, and the acid is concentrated sulfuric acid or concentrated hydrochloric acid.
Preferably, the acid leaching temperature in the step (3) is normal temperature, and the leaching time is 0.5-1 h.
Preferably, in the step (5), the alkali solution is NaOH solution, the concentration is 1-2mol/L, the alkali leaching temperature is 80-100 ℃, the leaching time is 4-5h, and the liquid-solid ratio of the slurry after the alkali leaching is (5-10): 1.
Preferably, the heating temperature in the step (8) is 45 ℃, and the stirring time is 10-30 min.
Preferably, the drying temperature in the step (9) is 120 ℃, and the time is 1 h.
Preferably, the roasting temperature in the step (9) is 300 ℃ and the time is 2 hours.
Preferably, the acid leaching residue and the alkali leaching residue obtained in the steps (4) and (6) are high-purity alumina having a purity of more than 90%, and are recovered and reused.
Preferably, in the step (10), the residual liquid obtained in the step (8) is returned to the ball milling process of the step (1) to realize circulation for 8-10 times, and then evaporation crystallization is carried out to prepare NaCl or Na2SO4And (5) producing the product.
Compared with the prior art, the invention has the following beneficial effects:
(1) by adopting the leaching mode, elements such as nitrogen, fluorine, sodium, aluminum and the like leached by the electrolytic aluminum ash are converted into ammonia water and electrolyte products, and high-purity alumina (namely acid leaching residue and alkali leaching residue) is obtained at the same time, and can be used as a raw material to prepare high-alumina brick refractory materials and other products, so that the additional value of the aluminum ash is improved, the pollution of waste water to the environment is avoided, the resource utilization is realized, zero emission is realized, and no secondary waste is generated;
(2) the residual fluorine solution after the electrolyte preparation is returned to the ball milling process, so that the circulation of wastewater is realized, the resource utilization of fluorine is further improved, and the fluorine emission is eliminated;
(3) the acid-base combined process effectively solves the problem of neutralization of a single acid process or alkali process, does not need to add extra alkali or acid to neutralize pickle liquor or alkali immersion liquor, can obviously reduce the acid-base consumption of unit secondary aluminum ash, greatly reduces the produced byproduct salt, greatly reduces the production cost, is easy for industrial implementation, and obviously improves the economic benefit of enterprises.
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FIG. 1 is a process flow diagram of the present invention.
Detailed Description
In order to make the technical problems, technical solutions and advantages of the present invention more apparent, the following detailed description is given with reference to the accompanying drawings and specific embodiments.
Aiming at the existing problems, the invention provides an acid-base combined process for completely realizing resource utilization of high-fluorine secondary aluminum ash, which comprises the following steps: ball-milling the high-fluorine secondary aluminum ash, screening to remove metallic aluminum, and dividing into A, B parts; mixing the A part with water, heating, stirring and leaching; mixing the slurry after water leaching with acid (concentrated sulfuric acid or concentrated hydrochloric acid), and stirring and leaching at normal temperature; carrying out solid-liquid separation on the slurry after acid leaching to obtain acid leaching solution and acid leaching residue; directly mixing B part of aluminum ash with an alkali solution, heating, stirring and leaching; carrying out solid-liquid separation on the slurry after alkaline leaching to obtain alkaline leaching solution and alkaline leaching residue; mixing the obtained acid leaching solution and the obtained alkali leaching solution according to a proper proportion, and enabling the pH value of the solution to be close to neutral; heating and stirring the obtained mixed solution, and carrying out solid-liquid separation to obtain electrolyte and residual liquid; washing the electrolyte for three times, drying and roasting to obtain an electrolyte product; returning the obtained residual liquid to the ball millEvaporating and crystallizing after the process is circulated for 8-10 times to prepare NaCl or Na2SO4And (5) producing the product.
The method comprises the steps of firstly, ball-milling the secondary aluminum ash by using a ball mill, and then, screening by using a sieve with the aperture of 0.074 mm. The water immersion temperature is 90-100 ℃, the time is 4-6h, and the liquid-solid ratio of water to aluminum ash is (4-6) to (1-2). The aluminum nitride is decomposed in hot water and dilute alkali solution, the higher the temperature is, the faster the decomposition rate is, and meanwhile, the faster the ammonia gas overflows from the leaching solution, and the overflowed ammonia gas is recovered to prepare an ammonia water product.
H after mixing of slurry and acid in acid leaching+The concentration is 2-4mol/L, the liquid-solid ratio of the slurry after acid leaching is (5-10) to 1, the acid leaching temperature is normal temperature, and the leaching time is 0.5-1 h; in the alkaline leaching, an alkaline solution is a NaOH solution, the concentration is 1-2mol/L, the alkaline leaching temperature is 80-100 ℃, the leaching time is 4-5h, the solid-to-liquid ratio of slurry after alkaline leaching is (5-10):1, the heating temperature of an acid-base mixed solution is 45 ℃, and the stirring time is 10-30 min; the drying temperature of the electrolyte is 120 ℃, the time is 1h, the roasting temperature is 300 ℃, and the time is 2 h. The whole process has no secondary waste, all elements in the high-fluorine secondary aluminum ash are fully utilized, substances with additional values such as electrolyte, ammonia water, high-purity alumina (namely acid leaching residue and alkali leaching residue), salts and the like are obtained, the full utilization of resources and zero emission of pollutants are realized, and products with high additional values are obtained.
Example 1
The specific operation is as follows:
(1) 3kg of secondary high-fluorine aluminum ash is subjected to ball milling by a ball mill and then is sieved, the yield on the sieve is 4.18 percent, the grade of metallic aluminum is 72.6 percent, the recovery rate is 71 percent, and the sieve is divided into two parts, namely A (958 g) and B (1916 g);
(2) adding A part of aluminum ash and water into a reaction kettle according to a liquid-solid ratio of 5:2, heating, stirring and leaching for 4 hours at 100 ℃, and recovering overflowed ammonia gas with water to prepare ammonia water;
(3) adding a proper amount of concentrated hydrochloric acid into the water leaching solution to prepare 3.5mol/L hydrochloric acid, and performing acid leaching, stirring and leaching according to the liquid-solid ratio of 5:1 at normal temperature for 1 h;
(4) and carrying out solid-liquid separation after acid leaching to obtain acid leaching residue and acid leaching solution. The yield of the acid leaching residue is 44.64 percent, and the acid leaching residue is alumina with the purity of more than 95 percent; the pickle liquor contains 18.49g/L of fluorine, 9.12g/L of sodium and 38.11g/L of aluminum;
(5) mixing B part of aluminum ash and 1.5mol/L NaOH solution according to a liquid-solid ratio of 5:1, directly heating and stirring at 100 ℃ to leach for 4 hours, and recovering overflowed ammonia gas with water to prepare ammonia water;
(6) carrying out solid-liquid separation on the slurry after alkaline leaching to obtain alkaline leaching residue and alkaline leaching solution, wherein the yield of the alkaline leaching residue is 84.37 percent, and the alkaline leaching residue is alumina with the purity of more than 90 percent; the alkali leaching solution contains 15.77g/L of fluorine, 44.62g/L of sodium and 15.47g/L of aluminum;
(7) respectively taking 4.5L of pickle liquor and 9L of alkaline pickle liquor (according to the ratio of 1: 2) according to acid-base neutralization balance calculation, and mixing the pickle liquor and the alkaline pickle liquor to obtain a mixture with the pH value of 7.5;
(8) stirring the mixed solution at 45 ℃ for 0.5h, filtering, washing for three times, drying the obtained solid at 120 ℃ for 2h, and roasting at 300 ℃ for 2h to obtain 741.5g of electrolyte (containing 25.3% of fluorine, 40.82% of aluminum, 0.42% of sodium, and the balance of oxygen and other trace elements);
(9) filtrate contains 0.52g/L fluorine, 32.44g/L sodium and 0.15g/L aluminum, is unsaturated, returns the filtrate to the ball milling process to realize circulation, and is evaporated and crystallized after being circulated for 8-10 times to prepare NaCl or Na2SO4And (5) producing the product.
Example 2
The specific operation is as follows:
(1) 2.3kg of secondary high-fluorine aluminum ash is subjected to ball milling and then is sieved by a ball mill, the yield on the sieve is 4.8 percent, the grade of metallic aluminum is 68.1 percent, the recovery rate is 76.55 percent, and the part A (952 g) and the part B (1247 g) are sieved;
(2) adding A part of aluminum ash and water into a reaction kettle according to a liquid-solid ratio of 5:2, heating, stirring and leaching for 4 hours at 100 ℃, and recovering overflowed ammonia gas with water to prepare ammonia water;
(3) adding a proper amount of concentrated hydrochloric acid into the water leaching solution to prepare 4mol/L hydrochloric acid, and performing acid leaching, stirring and leaching according to the liquid-solid ratio of 5:1 at normal temperature for 1 h;
(4) and carrying out solid-liquid separation after acid leaching to obtain acid leaching residue and acid leaching solution. The yield of the acid leaching residue is 43.52%, the acid leaching residue is alumina with the purity of more than 95%, and the acid leaching solution contains 19.56g/L of fluorine, 9.45g/L of sodium and 39.23g/L of aluminum;
(5) mixing B part of aluminum ash and 1.75mol/L NaOH solution according to a liquid-solid ratio of 5:1, directly heating and stirring at 100 ℃ to leach for 4 hours, and recovering overflowed ammonia gas with water to prepare ammonia water;
(6) and carrying out solid-liquid separation on the slurry after alkaline leaching to obtain alkaline leaching residue and alkaline leaching solution. The yield of the alkaline leaching residue is 79.8 percent, and the alkaline leaching residue is alumina with the purity of more than 90 percent; the alkali leaching solution contains 16.12g/L of fluorine, 49.83g/L of sodium and 17.45g/L of aluminum;
(7) respectively taking 4.5L of pickle liquor and 5.6L of alkaline pickle liquor (according to a ratio of 4: 5) according to acid-base neutralization balance calculation, and mixing, wherein the pH value is 5.6;
(8) stirring the mixed solution at 45 ℃ for 0.5h, filtering, washing for three times, drying the obtained solid at 120 ℃ for 2h, and roasting at 300 ℃ for 2 h; 528.7g of electrolyte (containing 24.25% of fluorine, 40.8% of aluminum, 0.4% of sodium and the balance of oxygen and other trace elements) is obtained;
(9) filtrate contains 1.19g/L fluorine, 31.78g/L sodium and 0.42g/L aluminum, is unsaturated, returns the filtrate to the ball milling process to realize circulation, and is evaporated and crystallized after being circulated for 8-10 times to prepare NaCl or Na2SO4And (5) producing the product.
Example 3
The specific operation is as follows:
(1) 2.4kg of secondary high-fluorine aluminum ash is subjected to ball milling and then sieved by a ball mill, the yield on the sieve is 3.94%, the grade of metallic aluminum is 73.5%, the recovery rate is 67.82%, and the part under the sieve is divided into two parts, namely A (960 g) and B (1325 g);
(2) adding A part of aluminum ash and water into a reaction kettle according to a liquid-solid ratio of 5:2, heating, stirring and leaching for 4 hours at 100 ℃, and recovering overflowed ammonia gas with water to prepare ammonia water;
(3) adding a proper amount of concentrated hydrochloric acid into the water leaching solution to prepare 2.25mol/L hydrochloric acid, and performing acid leaching, stirring and leaching according to the liquid-solid ratio of 10:1 at normal temperature for 1 h;
(4) and carrying out solid-liquid separation after acid leaching to obtain acid leaching residue and acid leaching solution. The yield of the acid leaching residue is 41.98%, the acid leaching residue is alumina with the purity of more than 95%, the dried acid leaching residue can be used as a raw material for preparing products such as high-alumina bricks and the like, and the acid leaching solution contains 9.95g/L of fluorine, 8.56g/L of sodium and 18.7g/L of aluminum;
(5) mixing B part of aluminum ash and 1.25mol/L NaOH solution according to a liquid-solid ratio of 10:1, directly heating and stirring at 100 ℃ to leach for 4 hours, and recovering overflowed ammonia gas with water to prepare ammonia water;
(6) and carrying out solid-liquid separation on the slurry after alkaline leaching to obtain alkaline leaching residue and alkaline leaching solution. The yield of the alkaline leaching residue is 63.13%, and the alkaline leaching residue is alumina with the purity of more than 90%; the alkali leaching solution contains 8.43g/L of fluorine, 40.62g/L of sodium and 14.85g/L of aluminum;
(7) respectively taking 9L of pickle liquor and 12L of alkaline pickle liquor (according to the ratio of 1: 1.35) according to acid-base neutralization balance calculation, and mixing, wherein the pH value is 7;
(8) stirring the mixed solution at 45 ℃ for 0.5h, filtering, washing for three times, drying the obtained solid at 120 ℃ for 2h, and roasting at 300 ℃ for 2 h; 820.5g of electrolyte (containing 20.344% of fluorine, 41.58% of aluminum, 0.24% of sodium and the balance of oxygen and other trace elements) is obtained;
(9) filtrate contains 0.43g/L fluorine, 26.89g/L sodium and 0.12g/L aluminum, is not saturated, returns the filtrate to the ore grinding process to realize circulation, and is evaporated and crystallized after being circulated for 8-10 times to prepare NaCl or Na2SO4And (5) producing the product.
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (9)
1. An acid-base combined process for completely realizing resource utilization of high-fluorine secondary aluminum ash is characterized by comprising the following steps:
(1) ball-milling the high-fluorine secondary aluminum ash, screening to remove metallic aluminum, and dividing into A, B parts of aluminum ash;
(2) mixing A part of aluminum ash with water, heating, stirring and leaching;
(3) mixing the slurry leached in the step (2) with acid, and stirring and leaching at normal temperature;
(4) carrying out solid-liquid separation on the slurry subjected to acid leaching in the step (3) to obtain acid leaching solution and acid leaching residue;
(5) directly mixing B part of aluminum ash with an alkali solution, heating, stirring and leaching;
(6) carrying out solid-liquid separation on the slurry obtained after the alkaline leaching in the step (5) to obtain an alkaline leaching solution and alkaline leaching residues;
(7) mixing the acid leaching solution obtained in the step (4) and the alkali leaching solution obtained in the step (6) in proportion, and then adjusting the pH value to 5-8;
(8) heating and stirring the mixed solution obtained in the step (7), and carrying out solid-liquid separation to obtain electrolyte and residual liquid;
(9) washing, drying and roasting the electrolyte obtained in the step (8) to obtain an electrolyte product;
(10) returning the residual liquid obtained in the step (8) to the ball milling process in the step (1) to realize circulation;
h after mixing the slurry and the acid in the acid leaching in the step (3)+The concentration is 2-4mol/L, the liquid-solid ratio of the slurry after acid leaching is (5-10) to 1, and the acid is concentrated sulfuric acid or concentrated hydrochloric acid.
2. The acid-base combined process as claimed in claim 1, wherein the water leaching temperature in the step (2) is 90-100 ℃, the water leaching time is 4-6h, and the liquid-solid ratio of water to aluminum ash is (4-6): 1-2.
3. The integrated acid-base process of claim 1, wherein steps (2) and (5) further comprise recovering ammonia gas generated in the water/alkali leaching process and preparing the ammonia gas into ammonia water.
4. The acid-base combined process according to claim 1, wherein the acid leaching temperature in the step (3) is normal temperature, and the leaching time is 0.5-1 h.
5. The acid-base combined process according to claim 1, wherein in the step (5), the alkali solution is NaOH solution, the concentration is 1-2mol/L, the alkali leaching temperature is 80-100 ℃, the leaching time is 4-5h, and the slurry liquid-solid ratio after alkali leaching is (5-10): 1.
6. The acid-base combined process according to claim 1, wherein the heating temperature in the step (8) is 45 ℃ and the stirring time is 10-30 min.
7. The acid-base combined process according to claim 1, wherein the drying temperature in the step (9) is 120 ℃ and the time is 1h, and the roasting temperature is 300 ℃ and the time is 2 h.
8. The acid-base combined process according to claim 1, wherein in the step (10), the residual liquid obtained in the step (8) is returned to the ball milling process in the step (1) for circulation for 8-10 times, and then evaporation crystallization is carried out to prepare NaCl or Na2SO4And (5) producing the product.
9. The integrated acid-base process according to claim 1, wherein the acid leaching residue and the alkali leaching residue obtained in the steps (4) and (6) are high-purity alumina with the purity of more than 90%.
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| CN111889489B (en) * | 2020-08-04 | 2022-04-22 | 郑州鸿跃环保科技有限公司 | Treatment method and treatment system for aluminum electrolysis overhaul slag |
| CN112553471B (en) * | 2020-12-22 | 2022-12-09 | 郑州中科新兴产业技术研究院 | Method for removing fluoride from aluminum ash by external field strengthening means |
| CN113072089B (en) * | 2021-03-26 | 2022-08-05 | 广西博世科环保科技股份有限公司 | Method for recovering cryolite by combined treatment of aluminum electrolysis overhaul slag and aluminum ash |
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| CN113426808B (en) * | 2021-06-29 | 2022-05-17 | 云南云铝润鑫铝业有限公司 | Method for recovering fluoride salt from aluminum electrolysis overhaul residues through pressurized alkaline leaching |
| CN113684369B (en) * | 2021-09-16 | 2022-06-14 | 中南大学 | Method for treating waste industrial lithium-containing aluminum electrolyte |
| CN114273382B (en) * | 2021-12-27 | 2023-04-07 | 山东东顺环保科技有限公司 | Harmless treatment method for secondary aluminum ash |
| CN115140719B (en) * | 2022-06-27 | 2024-03-01 | 中铝郑州有色金属研究院有限公司 | Method for full recycling of secondary aluminum ash |
| CN115286272A (en) * | 2022-08-24 | 2022-11-04 | 浙江红狮环保股份有限公司 | Technology for removing fluorine and chlorine from aluminum ash |
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| US4362703A (en) * | 1982-03-01 | 1982-12-07 | Iowa State University Research Foundation, Inc. | Process for preparing cryolite from fly ash |
| CN1254023A (en) * | 1999-06-12 | 2000-05-24 | 湖南省安化县碳化硅厂 | Leaching-out method for extracting vanadium from vanadium-containg ore calcines and its application in stone-coal calcination-direct vanadium-extracting process |
| JP2004154614A (en) * | 2002-11-01 | 2004-06-03 | Kobe Steel Ltd | Method for treating aluminum dross residual ash |
| CN103060566A (en) * | 2011-10-21 | 2013-04-24 | 湖南创元铝业有限公司 | Method for recovering aluminum oxide, chlorine salt and villiaumite from aluminum ash |
| CN103555955B (en) * | 2013-11-13 | 2015-04-22 | 昆明冶金研究院 | Resource utilization method of aluminum ash |
| CN105271327B (en) * | 2014-09-26 | 2017-04-05 | 昆明冶金研究院 | A kind of aluminum ash harmless treatment the method for recycling |
| CN106830025B (en) * | 2017-02-24 | 2018-06-19 | 南通大学 | aluminium ash recycling method |
| CN110304646B (en) * | 2019-07-15 | 2021-07-09 | 郑州中科新兴产业技术研究院 | Method for efficiently separating fluorine, chlorine and nitrogen components from aluminum ash and co-producing aluminum oxide concentrate |
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