CN110963515B - Method for recovering alumina from fly ash - Google Patents
Method for recovering alumina from fly ash Download PDFInfo
- Publication number
- CN110963515B CN110963515B CN201911378382.0A CN201911378382A CN110963515B CN 110963515 B CN110963515 B CN 110963515B CN 201911378382 A CN201911378382 A CN 201911378382A CN 110963515 B CN110963515 B CN 110963515B
- Authority
- CN
- China
- Prior art keywords
- nitric acid
- fly ash
- filtrate
- filtering
- stirring
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/20—Preparation of aluminium oxide or hydroxide from aluminous ores using acids or salts
- C01F7/24—Preparation of aluminium oxide or hydroxide from aluminous ores using acids or salts with nitric acid or nitrogen oxides
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a method for recovering alumina from fly ash, which comprises the following steps: step 1, mixing the fly ash powder with water, stirring and slurrying to obtain slurry. And 2, magnetically separating the slurry obtained in the step 1 by using a magnetic separator, and filtering to obtain filter residues. And 3, adding water into the filter residue obtained in the step 2, stirring and slurrying, then adding nitric acid, and stirring to obtain a mixed material. And 4, adding the mixed material obtained in the step 3 into a reaction kettle, heating, pressurizing to perform reaction, cooling and filtering to obtain a first filtrate. And 5, adding hydrogen peroxide into the first filtrate obtained in the step 4, adjusting the pH value to 3-3.5, reacting, and filtering to obtain a second filtrate. And 6, evaporating and concentrating the second filtrate obtained in the step 5 to obtain aluminum nitrate crystals. And 7, calcining and decomposing the aluminum nitrate crystal obtained in the step 6 to obtain the aluminum oxide, wherein the method has the advantages of low acid consumption, low impurity content in the leaching solution, low impurity removal cost, low equipment requirement, simple process and the like.
Description
Technical Field
The invention belongs to the technical field of alumina extraction, and particularly relates to a method for recovering alumina from fly ash.
Background
At present, coal is used in thermal power generation and heating plants in north China to generate a large amount of fly ash, the fly ash is used in the field of building materials, cement manufacturing and brick making, but the fly ash contains a large amount of aluminum oxide, silicon oxide and iron, and aluminum resources in China are very lacking, so that the utilization of the fly ash has a wide prospect.
The method for extracting the alumina from the fly ash can be divided into an acid method and an alkaline method, and the alkaline method has mature recovery process, but has long process flow and high recovery cost; the acid method comprises a hydrochloric acid method and a sulfuric acid method at present, the content of iron in the fly ash is high, the fly ash is directly leached by acid through the existing acid method recovery process, the iron in the fly ash almost completely enters a leaching solution, the acid consumption is high, the leaching cost is high, the content of iron impurities in the leaching solution is high, the impurity removal cost is high, meanwhile, in the hydrochloric acid process, the hydrogen chloride acidic gas is easy to volatilize, equipment is seriously corroded, and particularly, special materials are needed for pressure leaching equipment, so the investment cost is high; the sulfuric acid method leaching requires high leaching temperature and high pressure, and the safety requirement of leaching equipment is high.
Disclosure of Invention
Aiming at the problems of long process flow and high recovery cost of the alkaline method in the method for extracting the alumina from the fly ash in the prior art; the invention provides a method for recovering alumina from fly ash, which has the advantages of low acid consumption, low impurity content in leachate, low impurity removal cost, low equipment requirement, simple process and the like.
In order to achieve the above purpose, the invention provides the following technical scheme:
a method for recovering alumina from fly ash, comprising the steps of:
step 1, mixing the fly ash powder with water, stirring and slurrying to obtain slurry.
And 2, magnetically separating the slurry obtained in the step 1 by using a magnetic separator, and filtering to obtain filter residues.
And 3, adding water into the filter residue obtained in the step 2, stirring and slurrying, then adding nitric acid, and stirring to obtain a mixed material.
And 4, adding the mixed material obtained in the step 3 into a reaction kettle, heating, pressurizing to perform reaction, cooling and filtering to obtain a first filtrate.
And 5, adding hydrogen peroxide into the first filtrate obtained in the step 4, adjusting the pH value to 3-3.5, reacting, and filtering to obtain a second filtrate.
And 6, evaporating and concentrating the second filtrate obtained in the step 5 to obtain aluminum nitrate crystals.
And 7, calcining and decomposing the aluminum nitrate crystal obtained in the step 6 to obtain aluminum oxide.
The invention provides a method for recovering alumina from fly ashThe method comprises the steps of firstly, magnetically separating the fly ash to obtain a magnetic material containing a large amount of iron, wherein the material contains higher iron, treating a non-magnetic material by adopting a nitric acid leaching process, enabling aluminum in alumina to exist in a solution in the form of aluminum ions, enabling silicon dioxide to exist in the filtered out material, then adding hydrogen peroxide to oxidize ferrous iron under an acidic condition, and oxidizing the ferrous iron into ferric iron based on the oxidation of the ferrous iron, wherein Fe (OH) is generated when the hydrolysis pH value of the ferric iron is lower3Precipitating and filtering to obtain an aluminum nitrate solution, evaporating and concentrating to obtain aluminum nitrate crystals, and calcining the aluminum nitrate crystals to obtain the aluminum oxide. The acid of the method is not needed to be used for leaching a large amount of iron, and the method has the advantages of low acid consumption, low impurity content of the leaching solution, low impurity removal cost, low requirement on equipment and simple process.
Further, the particle size of the fly ash powder in the step 1 is 200-500 meshes. Preferably, the particle size of the fly ash in step 1 is 300 to 500 meshes. The selection of the proper particle size of the fly ash is directly related to the slurry state of the slurry, and in the subsequent recovery process, the over-large or over-small particle size of the fly ash is not beneficial to the reaction with the nitric acid, and the efficiency of the nitric acid can be influenced.
Further, in the step 1, the weight volume ratio of the fly ash powder to the water is 100 g: 300ml to 500 ml. And the proper liquid-solid ratio is selected, so that the efficiency of the recovery process is increased.
Further, the magnetic flux of the magnetic separator in the step 2 is 6000 gauss-12000 gauss. Preferably, the magnetic flux of the magnetic separator in the step 2 is 9000 gauss to 12000 gauss, and the selection of a proper magnetic flux is favorable for improving the quality of the separated magnetic materials and avoiding resource waste.
Further, the process parameters in step 3 are as follows: the weight volume ratio of the filter residue to the water is 100 g: 300ml to 500 ml; the nitric acid is a nitric acid solution with the mass fraction of 30-60%, and the addition amount of the nitric acid is 1.1-1.5 times of the theoretical addition amount of the nitric acid.
Further, the addition amount of nitric acid in step 3 is 1.2 to 1.35 times the theoretical addition amount of nitric acid. The inventor unexpectedly finds that the addition amount of the nitric acid is higher than the theoretical addition amount by a certain amount, so that the reaction end point solution keeps a certain acid amount, and the leaching rate of the alumina is favorably improved. The theoretical nitric acid addition amount is calculated by using the content of the alumina in the filter residue.
Further, the process parameters in the step 4 are as follows: the temperature is 130-180 ℃, the pressure is 0.3-0.8 MPa, and the reaction time is 1-4 h. Preferably, the temperature is 150 ℃ to 170 ℃.
Further, the temperature in the step 4 is 150-170 ℃. The inventor finds that the temperature has great influence on the recovery rate of alumina, the efficiency of leaching the fly ash by nitric acid is influenced by too low or too high temperature, and the recovery rate of the alumina is more than 93% at 130-180 ℃, preferably more than 95% at 150-170 ℃.
Further, the reaction temperature in the step 5 is 70-90 ℃.
Further, the evaporation concentration process condition in the step 6 is 60 ℃ to 100 ℃, preferably, the evaporation concentration process condition in the step 6 is 90 ℃ to 100 ℃.
Further, step 7, melting the aluminum nitrate crystal into liquid at 100-120 ℃, pumping into an atomization decomposing furnace, contacting with circulating nitrogen oxide gas at 800-. The gas released by decomposition is NO2、NO、O2、H2And (3) recycling a part of the O mixed gas into the heat storage furnace to be heated, and enabling the rest of the O mixed gas to enter a nitric acid absorption device to obtain nitric acid with a certain concentration, wherein the concentration of the nitric acid is 30-60%, the nitric acid is used for front-stage leaching, and the tail gas is less than 100ppm and is discharged after reaching the standard.
Furthermore, the content of alumina in the fly ash powder is 10-50%, and the content of iron is 5-20%.
Compared with the prior art, the invention has the beneficial effects that:
1. the invention provides a method for recovering alumina from fly ash, which comprises the steps of firstly magnetically separating the fly ash to obtain magnetic materials containing a large amount of iron, and then leaching nonmagnetic materials by nitric acid.
2. The invention provides a method for recovering alumina from fly ash, which ensures that the whole process has good recovery rate of alumina by controlling the temperature and the addition amount of nitric acid in the nitric acid leaching process, and the recovery rate can reach more than 98 percent.
3. The invention provides a method for recovering alumina from fly ash, the leaching temperature and pressure of the method are lower than those of sulfuric acid leaching, and the decomposition and recovery of an intermediate product, namely aluminum nitrate, are easier to realize industrialization.
Detailed Description
The present invention will be described in further detail with reference to test examples and specific embodiments. It should be understood that the scope of the above-described subject matter is not limited to the following examples, and any techniques implemented based on the disclosure of the present invention are within the scope of the present invention. The percentages not specifically stated in the present invention generally refer to weight percentages.
Note: the fly ashes in the following examples are all purchased from the same batch, wherein the fly ashes comprise alumina: 45% of Fe3O4：10％、SiO2：38％、CaO：2％、MgO：2％。
Example 1
Grinding 10kg of purchased fly ash, sieving the ground fly ash by a sieve of 300 meshes, adding 3L of water, stirring and slurrying, then carrying out magnetic separation on the slurry by a magnetic separator of 800 gauss, separating out magnetic materials, and then filtering the slurry to obtain nonmagnetic materials. The non-magnetic material is mixed according to the liquid-solid ratio of 400 ml: mixing 100g of the mixture with water, stirring and slurrying, adding nitric acid which is 1.2 times of the theoretical addition amount of the nitric acid into the slurry, introducing the slurry into a reaction kettle, reacting for 2 hours at 160 ℃ under the pressure of 0.62MPa, relieving pressure and cooling after the reaction is finished, filtering, wherein filter residues contain a large amount of silicon dioxide and can be sold in a cement plant; adding hydrogen peroxide into filtrate, wherein 0.8-1.8 kg of 27% industrial grade hydrogen peroxide is needed for every 1 kg of ferrous, the hydrogen peroxide is diluted by 1 time and added, the pH value is adjusted to be 3.2, filtering is carried out again, then the filtrate is evaporated, concentrated and crystallized to obtain aluminum nitrate crystals, then the aluminum nitrate crystals are decomposed in an atomization decomposing furnace at 900 ℃, the upper nitrogen oxide mixed gas enters a nitric acid absorption device to be absorbed into nitric acid with the concentration of 30-60% for recycling, the lower part of the decomposing furnace collects aluminum oxide, the recovery rate of the aluminum oxide is 95% by calculation, and the aluminum oxide is used for further smelting into electrolytic aluminum.
Example 2
10kg of purchased fly ash is ground, sieved by a 350-mesh sieve, added with 3L of water, stirred and pulped, then magnetically separated by a 900-gauss magnetic separator to separate out magnetic materials, and then the slurry is filtered to obtain nonmagnetic materials. And (3) mixing the nonmagnetic material according to the liquid-solid ratio of 350 ml: mixing 100g of the mixture with water, stirring and slurrying, adding nitric acid which is 1.13 times of the theoretical addition amount of the nitric acid into the slurry, introducing the slurry into a reaction kettle, reacting for 2 hours at 130 ℃ under the pressure of 0.62MPa, relieving pressure and cooling after the reaction is finished, filtering, wherein filter residues contain a large amount of silicon dioxide and can be sold in a cement plant; adding hydrogen peroxide into filtrate, wherein 0.8-1.8 kg of 27% industrial grade hydrogen peroxide is needed for every 1 kg of ferrous iron, diluting the hydrogen peroxide by 1 time, adjusting the pH value to 3.2, filtering again, evaporating, concentrating and crystallizing the filtrate to obtain aluminum nitrate crystals, decomposing the aluminum nitrate crystals in an atomization decomposing furnace at 1000 ℃, allowing the upper nitrogen oxide mixed gas to enter a nitric acid absorption device to be absorbed into nitric acid with the concentration of 30-60% for recycling, collecting aluminum oxide at the lower part of the decomposing furnace, and calculating the recovery rate of the aluminum oxide to be 94.2%, wherein the aluminum oxide is used for further smelting into electrolytic aluminum.
Example 3
Grinding 10kg of purchased fly ash, sieving the ground fly ash by a sieve of 400 meshes, adding 3L of water, stirring and slurrying, then carrying out magnetic separation on the slurry by a magnetic separator of 900 gauss, separating out magnetic materials, and then filtering the slurry to obtain nonmagnetic materials. The non-magnetic material is mixed according to the liquid-solid ratio of 450 ml: mixing 100g of the mixture with water, stirring and slurrying, adding nitric acid which is 1.32 times of the theoretical addition amount of the nitric acid into the slurry, introducing the slurry into a reaction kettle, reacting for 2 hours at 180 ℃ and under the pressure of 0.62MPa, relieving pressure and cooling after the reaction is finished, filtering, wherein filter residues contain a large amount of silicon dioxide and can be sold in a cement plant; adding hydrogen peroxide into filtrate, wherein 0.8-1.8 kg of 27% industrial grade hydrogen peroxide is needed for every 1 kg of ferrous iron, diluting the hydrogen peroxide by 1 time, adjusting the pH value to 3.2, filtering again, evaporating, concentrating and crystallizing the filtrate to obtain aluminum nitrate crystals, decomposing the aluminum nitrate crystals in an atomization decomposing furnace at 950 ℃, allowing the upper nitrogen oxide mixed gas to enter a nitric acid absorption device to be absorbed into nitric acid with the concentration of 30-60% for recycling, collecting aluminum oxide at the lower part of the decomposing furnace, and calculating the recovery rate of the aluminum oxide to be 95.7%, wherein the aluminum oxide is used for further smelting into electrolytic aluminum.
Examples 4 to 12
The reaction temperature and the actual addition amount of nitric acid in the reaction kettle in the process of recovering alumina from fly ash in examples 4-12 are shown in table 1, the other recovery process parameters, raw material ratios, experimental processes and the like are the same as those in example 1, and the recovery rate of alumina is calculated for the recovery of alumina in examples 4-12 and is also shown in table 1.
Table 1 examples 4-12 recovery process parameters and recovery of alumina
As can be seen from the alumina recovery rates in Table 1, the temperature has a great influence on the alumina recovery rate, and the efficiency of leaching the fly ash by nitric acid is affected by too low or too high temperature, and the alumina recovery rate is more than 93% at 130-180 ℃, preferably more than 95% at 150-170 ℃.
Examples 13 to 21
The reaction temperature and the actual addition amount of nitric acid in the reaction kettle in the process of recovering alumina from fly ash in examples 13-21 are shown in table 2, the other recovery process parameters, raw material ratios, experimental procedures and the like are the same as those in example 1, and the recovery rate of alumina from the recovery of alumina in examples 13-21 is calculated and is also shown in table 2.
Table 2 examples 13-21 recovery process parameters and recovery of alumina
Through a great deal of experimental research by the inventor, the addition amount of the nitric acid is higher than the theoretical addition amount by a certain amount, so that the solution at the end point of the reaction keeps a certain amount, which is beneficial to improving the leaching rate of the alumina, and as can be seen from the test data of the embodiment in table 2, when the addition amount of the nitric acid is 1.1-1.5 times of the theoretical addition amount of the nitric acid, the recovery rate of the alumina is between 94-98.1%, and preferably, the addition amount of the nitric acid is 1.2-1.35 times of the theoretical addition amount of the nitric acid, so that the alumina keeps an optimal recovery rate.
Example 22
10kg of purchased fly ash is ground, sieved by a 350-mesh sieve, added with 3L of water, stirred and pulped, then magnetically separated by a 900-gauss magnetic separator to separate out magnetic materials, and then the slurry is filtered to obtain nonmagnetic materials. And (3) mixing the nonmagnetic material according to the liquid-solid ratio of 350 ml: mixing 100g of the mixture with water, stirring and slurrying, adding nitric acid which is 1.24 times of the theoretical addition amount of the nitric acid into the slurry, introducing the slurry into a reaction kettle, reacting for 2 hours at 153 ℃ under the pressure of 0.62MPa, relieving pressure and cooling after the reaction is finished, filtering, wherein filter residues contain a large amount of silicon dioxide and can be sold in a cement plant; adding hydrogen peroxide into filtrate, wherein 0.8-1.8 kg of 27% industrial grade hydrogen peroxide is needed for every 1 kg of ferrous iron, diluting the hydrogen peroxide by 1 time, adjusting the pH value to 3.2, filtering again, evaporating, concentrating and crystallizing the filtrate to obtain aluminum nitrate crystals, decomposing the aluminum nitrate crystals in an atomization decomposing furnace at 1000 ℃, allowing the upper nitrogen oxide mixed gas to enter a nitric acid absorption device to be absorbed into nitric acid with the concentration of 30-60% for recycling, collecting aluminum oxide at the lower part of the decomposing furnace, and calculating the recovery rate of the aluminum oxide to be 98.2%, wherein the aluminum oxide is used for further smelting into electrolytic aluminum.
Example 23
10kg of purchased fly ash is ground, sieved by a 350-mesh sieve, added with 3L of water, stirred and pulped, then magnetically separated by a 900-gauss magnetic separator to separate out magnetic materials, and then the slurry is filtered to obtain nonmagnetic materials. And (3) mixing the nonmagnetic material according to the liquid-solid ratio of 350 ml: mixing 100g of the mixture with water, stirring and slurrying, adding nitric acid which is 1.33 times of the theoretical addition amount of the nitric acid into the slurry, introducing the slurry into a reaction kettle, reacting at 167 ℃ under the pressure of 0.62MPa for 2 hours, relieving pressure and cooling after the reaction is finished, filtering, wherein filter residues contain a large amount of silicon dioxide and can be sold in a cement plant; adding hydrogen peroxide into filtrate, wherein 0.8-1.8 kg of 27% industrial grade hydrogen peroxide is needed for every 1 kg of ferrous iron, diluting the hydrogen peroxide by 1 time, adjusting the pH value to 3.2, filtering again, evaporating, concentrating and crystallizing the filtrate to obtain aluminum nitrate crystals, decomposing the aluminum nitrate crystals in an atomization decomposing furnace at 1000 ℃, allowing the upper nitrogen oxide mixed gas to enter a nitric acid absorption device to be absorbed into nitric acid with the concentration of 30-60% for recycling, collecting aluminum oxide at the lower part of the decomposing furnace, and calculating the recovery rate of the aluminum oxide to be 98.4%, wherein the aluminum oxide is used for further smelting into electrolytic aluminum.
The invention relates to a method for recovering alumina from fly ash, which comprises the steps of firstly magnetically separating the fly ash to obtain a magnetic material containing a large amount of iron, and then leaching the non-magnetic material by nitric acid, wherein the acid in the method is not required to be used for leaching the large amount of iron, and the method has the advantages of low acid consumption, low impurity content of leachate, low impurity removal cost, low equipment requirement and simple process, researches show that the reaction temperature in a reaction kettle and the addition amount of nitric acid have close influence on the recovery rate of alumina, and the whole process has good recovery rate of alumina which can reach more than 98% by controlling process parameters.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (2)
1. A method for recovering alumina from fly ash is characterized by comprising the following steps:
step 1, mixing fly ash powder with water, stirring and slurrying to obtain slurry; the particle size of the fly ash powder is 200-500 meshes;
step 2, magnetically separating the slurry obtained in the step 1 by using a magnetic separator, and filtering to obtain filter residues; the magnetic flux of the magnetic separator is 6000 gauss-12000 gauss;
step 3, adding water into the filter residue obtained in the step 2, stirring and slurrying, then adding nitric acid, and stirring to obtain a mixed material; the weight volume ratio of the filter residue to the water is 100 g: 300ml to 500 ml; the nitric acid is a nitric acid solution with the mass fraction of 30-60%, and the addition amount of the nitric acid is 1.2-1.35 times of the theoretical addition amount of the nitric acid;
step 4, adding the mixed material obtained in the step 3 into a reaction kettle, heating, pressurizing to perform reaction, cooling and filtering to obtain a first filtrate; the temperature is 150-170 ℃, the pressure is 0.3-0.8 MPa, and the reaction time is 1-4 h;
step 5, adding hydrogen peroxide into the first filtrate obtained in the step 4, adjusting the pH value to 3-3.5, reacting, and filtering to obtain a second filtrate;
step 6, evaporating and concentrating the second filtrate obtained in the step 5 to obtain aluminum nitrate crystals; the evaporation concentration process condition is 60-100 ℃;
and 7, melting the aluminum nitrate crystal obtained in the step 6 into a liquid state at the temperature of 100-120 ℃, pumping the liquid into an atomization decomposing furnace, contacting with circulating nitrogen oxide gas at the temperature of 800-1000 ℃, calcining and decomposing for 1-30 min, and cooling to obtain the aluminum oxide.
2. The method of claim 1, wherein the fly ash has an alumina content of 10% to 50% and an iron content of 5% to 20%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911378382.0A CN110963515B (en) | 2019-12-27 | 2019-12-27 | Method for recovering alumina from fly ash |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911378382.0A CN110963515B (en) | 2019-12-27 | 2019-12-27 | Method for recovering alumina from fly ash |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110963515A CN110963515A (en) | 2020-04-07 |
| CN110963515B true CN110963515B (en) | 2021-09-10 |
Family
ID=70036975
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911378382.0A Active CN110963515B (en) | 2019-12-27 | 2019-12-27 | Method for recovering alumina from fly ash |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110963515B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111777087A (en) * | 2020-08-04 | 2020-10-16 | 眉山顺应动力电池材料有限公司 | System and method for producing alumina from coal gangue |
| CN112939046A (en) * | 2021-02-26 | 2021-06-11 | 四川顺应动力电池材料有限公司 | Comprehensive recycling method of coal-based solid waste |
| CN113401928B (en) * | 2021-06-15 | 2022-09-20 | 眉山顺应循环再生资源有限公司 | Method for removing calcium from fly ash and/or coal gangue by acid washing with ultrasonic waves |
| CN113582213A (en) * | 2021-07-26 | 2021-11-02 | 四川顺应动力电池材料有限公司 | Method for comprehensively utilizing fly ash |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1306940A (en) * | 2000-02-04 | 2001-08-08 | 赫多特普索化工设备公司 | Method for preparing aluminium oxide |
| CN105776345A (en) * | 2016-01-29 | 2016-07-20 | 卓达新材料科技集团有限公司 | Method for separating Fe2O3 in pulverized coal ash of pulverized coal furnace |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101863498A (en) * | 2010-04-27 | 2010-10-20 | 中国神华能源股份有限公司 | Method for recycling acid in process of producing alumina from fly ash by acid method |
| CN110395755A (en) * | 2019-09-05 | 2019-11-01 | 东北大学 | A method of aluminium oxide is produced using flyash |
-
2019
- 2019-12-27 CN CN201911378382.0A patent/CN110963515B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1306940A (en) * | 2000-02-04 | 2001-08-08 | 赫多特普索化工设备公司 | Method for preparing aluminium oxide |
| CN105776345A (en) * | 2016-01-29 | 2016-07-20 | 卓达新材料科技集团有限公司 | Method for separating Fe2O3 in pulverized coal ash of pulverized coal furnace |
Non-Patent Citations (1)
| Title |
|---|
| "粉煤灰硫酸焙烧熟料溶出液的除铁过程研究";刘康等;《中南大学学报(自然科学版)》;20161031;第47卷(第10期);第3296页左栏第1段至第3299页左栏第2段 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110963515A (en) | 2020-04-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110963515B (en) | Method for recovering alumina from fly ash | |
| CN110885090A (en) | Method for preparing battery-grade lithium carbonate by using lepidolite as raw material through one-step method | |
| CN109110826B (en) | Production method of battery-grade nickel sulfate | |
| CN112662896B (en) | Method for preparing titanium-rich material from titanium ore | |
| CN115583641B (en) | Method for preparing battery-grade ferric phosphate by cooperation of pyrite cinder and waste lithium iron phosphate battery cell | |
| CN114684801B (en) | Method for preparing high-purity ferric phosphate by using pyrite cinder | |
| CN112520790A (en) | Method for producing cobalt sulfate by using organic cobalt slag of zinc smelting plant | |
| CN114293035A (en) | Method for preparing calcium carbonate by enriching vanadium from vanadium-containing steel slag | |
| CN113582213A (en) | Method for comprehensively utilizing fly ash | |
| CN111187927A (en) | Method for selectively sulfating and recovering rare earth in neodymium iron boron waste | |
| CN114988485B (en) | Method for synchronously producing manganous-manganic oxide and ferric oxide for soft magnetism by using marine polymetallic nodule | |
| CN115259230A (en) | Impurity removal method for producing trimanganese tetroxide for soft magnetism from electrolytic manganese anode mud by utilizing molten acid leaching | |
| WO2023185056A1 (en) | Preparation method for iron phosphate and preparation method for lithium iron phosphate | |
| CN113149075A (en) | Method for preparing niobium pentoxide from low-grade niobium ore | |
| CN102634668A (en) | Roasting-free evaporation-free method for producing cupric sulfate from zinc hydrometallurgy acid-wash copper dross | |
| CN111074076B (en) | Comprehensive utilization system and method for metallurgical solid waste | |
| CN112993428A (en) | Method for recycling waste ternary lithium battery positive electrode material | |
| CN112391537B (en) | Method for extracting vanadium by using hydrochloric acid, sulfuric acid and vanadium-containing high-calcium high-phosphorus slag | |
| CN106702165B (en) | A method of leaching niobium scandium from tailing | |
| CN106892455B (en) | The green clean method for preparing of vanadium compounds | |
| CN102659167B (en) | Method for preparing copper sulfate from copper-containing material without evaporating | |
| CN105983707A (en) | Method for preparing high-purity rhenium powder from rhenium-containing high-arsenic copper sulfide | |
| CN108063295A (en) | The method that lithium is extracted in the clinker generated from pyrogenic process recycling lithium battery | |
| CN110117721B (en) | Method for extracting valuable metals from sulfuric acid residue by phosphoric acid leaching-extraction | |
| CN112111647B (en) | Method for pre-treating gold leaching by using gold ore calcine or roasting cyanidation tailings |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 620010 No. 1 Jinhua Road, Meishan high tech Industrial Park, Dongpo District, Meishan City, Sichuan Province Applicant after: Sichuan compliance power battery materials Co.,Ltd. Address before: 620020 Meishan Jinxiang Chemical Industrial Park, Meishan City, Sichuan Province Applicant before: MEISHAN SHUNYING POWER BATTERY MATERIAL Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20211123 Address after: 620000 Jinxiang Chemical Industrial Park, Meishan City, Sichuan Province Patentee after: Meishan compliance Recycling Resources Co.,Ltd. Address before: 620010 No. 1 Jinhua Road, Meishan high tech Industrial Park, Dongpo District, Meishan City, Sichuan Province Patentee before: Sichuan compliance power battery materials Co.,Ltd. |