CN115504494A - Salt-containing solid waste resource recovery method - Google Patents
Salt-containing solid waste resource recovery method Download PDFInfo
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- CN115504494A CN115504494A CN202211114695.7A CN202211114695A CN115504494A CN 115504494 A CN115504494 A CN 115504494A CN 202211114695 A CN202211114695 A CN 202211114695A CN 115504494 A CN115504494 A CN 115504494A
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- 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
- C01F7/48—Halides, with or without other cations besides aluminium
- C01F7/56—Chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
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- 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
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/20—Halides
- C01F11/24—Chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G49/00—Compounds of iron
- C01G49/10—Halides
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B21/00—Obtaining aluminium
- C22B21/0038—Obtaining aluminium by other processes
- C22B21/0069—Obtaining aluminium by other processes from scrap, skimmings or any secondary source aluminium, e.g. recovery of alloy constituents
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/20—Obtaining alkaline earth metals or magnesium
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/001—Dry processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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Abstract
The invention discloses a method for recycling salt-containing solid waste, which relates to the technical field of solid waste treatment, and comprises the steps of grinding, selecting powder, mixing and homogenizing, reducing and chlorinating, recovering calcium and iron, recovering aluminum-containing materials and recovering salt.
Description
Technical Field
The invention relates to the technical field of solid waste treatment, in particular to a method for recycling salt-containing solid waste.
Background
At present, the utilization of salt-containing solid waste has the following problems: (1) the temperature of the high-temperature method is 800-1000 ℃, a large amount of energy is needed for supporting, and the method is limited under the control of a double-carbon target; (2) the solid waste contains more calcium and iron, a large amount of waste residues are generated in the traditional chemical treatment process, and the problem that the treatment of the residues cannot be solved is a main technical bottleneck; (3) the separation cost of potassium and sodium salts generated in the impurity treatment process is high, and the mixed impurities cannot be removed, so that the potassium and sodium salts can only be treated as hazardous wastes, and the treatment cost is high.
Disclosure of Invention
Aiming at the technical problems, the invention overcomes the defects of the prior art and provides a method for recycling salt-containing solid waste, which comprises the following steps:
(1) Grinding and selecting powder
Unpacking aluminum ash, conveying the aluminum ash into an underground buffer hopper from the lower part of the buffer hopper through a scale and a large-inclination-angle belt, conveying the aluminum ash into a grinding and powder selecting integrated system, grinding and synchronously selecting powder, then conveying fine particles into a material mixing and homogenizing system through the scale and a lifting machine, discharging coarse particles from the grinding system, and performing closed-loop circulation through the scale and a screw conveyor to enter the underground buffer hopper;
(2) Homogenizing mixed material
The fine particles in the step (1) enter a material mixing and homogenizing system, are fully homogenized with waste salt powder in a double-shaft mixer, and the homogenized fine particles are discharged from the lower part of the homogenizing system through a discharging machine and enter a reactor;
(3) Reductive chlorination
Feeding the homogenized material in the step (2) into molten salt from a feed inlet at the upper part of the reactor, blowing chlorine gas at the lower part of the reactor into a reaction chamber to react with the molten salt, discharging the reacted flue gas from the upper part of the reactor, and discharging the molten salt from the lower part of the reactor;
(4) Recovery of calcium and iron
In the step (3), the fused salt is mixed with chlorine blown into the bottom in the high-temperature filtering chamber, the cooled solid material is suspended at the upper part of the fused salt and is discharged from an overflow port, the calcium and iron material is recovered, the heated chlorine is discharged from the upper part of the filtering chamber and is blown into the reaction chamber, and the fused salt is returned to the reaction chamber by a fused salt pump;
(5) Recovering the aluminum-containing material
Discharging the flue gas in the step (4), feeding the flue gas into a flue gas filtering chamber, separating aluminum chloride through a porous filtering pipe, feeding the separated flue gas into a rear-end desulfurization and denitrification treatment system, and returning the residual chlorine gas to the high-temperature filtering chamber for preheating;
(6) Salt recovery
And (4) discharging the excess molten salt in the system in the step (4) into a stirring tank, mixing the excess molten salt with water to form high-salt water, allowing the high-salt water to enter a salt recovery system, and crystallizing by using a triple-effect evaporator to obtain the sodium chloride potassium chloride salt mixed salt material.
The technical scheme of the invention is further defined as follows:
in the method for recycling the salt-containing solid waste, in the step (1), a ball mill is adopted for grinding, the size of a feed inlet of the ball mill is 300-500mm, the ball mill is provided with a 2-3 bin structure, the grinding speed is 5-10r/min, a grinding body adopts 20cm and 5cm high-strength zirconia balls, and a large ball and a small ball are assembled into 1 bin: 1-4: 2:1-1:5, if 3 bins exist: 1:5-1:10.
In the method for recycling the salt-containing solid waste, in the step (1), a dynamic powder concentrator is adopted to concentrate the powder at a discharge port of a ball mill; the angle of the guide vane is 30-45 degrees, the speed of the rotor is 250-550rpm, and the size D50 of the obtained fine material is less than 0.5mm.
In the method for recycling the salt-containing solid waste, in the step (2), the ratio of the aluminum ash to the waste salt entering the double-shaft mixer is 4:1-1:1.
In the method for recycling the salt-containing solid waste, in the step (3), the reaction chamber is in the form of a molten salt furnace, and the highest refractory temperature is 1100 DEG o C; the concentration of the chlorine is 50-20%, the balance gas is nitrogen, the oxygen content is less than 2%, the wind pressure is 5000-9000Pa, and the retention time of the molten salt is 30-60min(ii) a The deoxidation reducing agent is powdered carbon or sulfur.
In the method for recycling the salt-containing solid waste, in the step (4), the chlorine flow rate is introduced into the high-temperature filter chamber to be 10000-40000m 3 The temperature of the flue gas outlet is 900-1000 ℃.
In the method for recycling the salt-containing solid waste, in the step (5), a waste heat boiler is adopted to recover heat before a filtering chamber, the dust-containing flue gas is filtered by a porous industrial ceramic tube, and the filtering temperature is 200-400 ℃.
In the method for recycling the salt-containing solid waste, in the step (6), the water flow speed of the stirring tank is 1.4-3.7m/h, and the pH value is adjusted to 7-8 by sodium hydroxide.
In the method for recycling the salt-containing solid waste, in the steps (1) to (6), air locking valves are arranged at the discharge ports of the solid materials to prevent gas leakage, the system connection adopts closed equipment or a dust collector, and the system valves adopt the interlocking function of an electric control valve and the system.
The invention has the beneficial effects that:
(1) The method utilizes the characteristic that a large amount of heat is released in the chlorination process of AlN and Al metals in the reaction process of aluminum ash and chlorine, mixes the aluminum ash and waste salt under the condition of no external heat, converts elements in materials into mixed chlorides through reduction chlorination reaction, forms eutectic molten salt by the mixed chlorides at high temperature, further melts oxides such as aluminum oxide, iron oxide, calcium oxide and the like, and chlorine gas rapidly reacts with the oxides in the molten body, and the solid-liquid reaction accelerates the conversion of the oxides to the chlorides and is uniform in reaction;
(2) The method realizes the comprehensive utilization of green low-carbon salt-containing solid waste, converts stable impurities such as ferric oxide and the like into ferric chloride through high-temperature chlorination in the process, separates iron impurities by utilizing the temperature-condensation effect, and realizes the purification of products;
(3) The invention can further purify sodium chloride and potassium chloride, improve the salt quality, reduce the cost of salt separation and realize the high value-added utilization of industrial salt.
Drawings
FIG. 1 is a flow chart of the present invention.
Detailed Description
Example 1
The raw material aluminum ash is taken from a certain regenerated aluminum plant, the content of aluminum oxide is 58.3 percent, the content of metal aluminum is 4.2 percent, the content of ferric oxide is 4.1 percent, the content of calcium oxide is 1.4 percent, the content of nitride is 15.8 percent, the content of carbon is 2.0 percent, and the grain size D50=1.88mm. Get into underground formula buffering fill after the aluminium ash bale breaking, carry by the big inclination belt in buffering fill lower part and get into the ball mill, ball mill feed inlet size 300mm sets up 3 storehouse structures, and the grinding speed 10r/min, grinding body adopt 20cm and 2cm high strength zirconia ball, and big ball bobble collection is joined in marriage and is 1 storehouse: 10, 1,2 bins: 2, 1,3 bins: 1:10. The angle of the guide vane of the dynamic powder concentrator at the discharge port is 45 degrees, and the speed of the rotor is 550rpm. A fines size D50=0.33mm was obtained. The coarse material discharged from the feed opening of the ball mill returns to the feed opening of the ball mill for further grinding.
The waste salt comes from a certain chemical area, and has the chloride content of 87.3 percent and the carbon content of 4.2 percent. The waste salt and the aluminum ash fine powder are fed into a double-shaft mixer to be mixed, and the proportion is 4:1. The mixed materials enter a reactor, the feeding amount is 500kg/h, the chlorine concentration is 20%, the oxygen content is kept at 1%, the wind pressure is 5000Pa, the molten salt retention time is 60min, and carbon powder is added as a deoxidizing and reducing agent. After the reaction, the flue gas enters a flue gas filtering chamber after heat is recovered by a waste heat boiler, the filtering temperature is 400 ℃, and powdery aluminum chloride is obtained, the yield is 730kg/h, the purity is 97.3 percent, and the aluminum recovery rate reaches 98 percent. Molten salt enters a high-temperature filter chamber after reaction, residual chlorine in flue gas after desulfurization and denitrification is introduced into the high-temperature filter chamber for preheating, and the chlorine flow is 10000m 3 H, the temperature of the flue gas outlet is 700 ℃. After the temperature of the fused salt is reduced, the solid material is suspended at the upper part of the fused salt and is discharged from an overflow port, and the yield of the recovered material is 20kg/h, wherein the content of ferric chloride is 63 percent, and the content of calcium chloride is 27 percent. And the molten salt discharged from the high-temperature filter chamber is pumped into the reactor again through a molten salt pump for recycling. The remaining molten salt was discharged into a stirred tank, mixed with water to form a brine, stirred for Chi Liusu 3.7.7 m/h, adjusted to pH7 with sodium hydroxide. The salt-containing water enters a desalting system to generate 138kg/h of sodium chloride and potassium chloride mixed salt with chloride content of 94 percent.
Example 2
The raw material aluminum ash is taken from a certain regenerated aluminum plant, the content of aluminum oxide is 57.2 percent, the content of metal aluminum is 5.3 percent, the content of ferric oxide is 8.3 percent, the content of calcium oxide is 2.8 percent, the content of nitride is 22.3 percent, the content of carbon is 1.2 percent, and the grain size D50=0.92mm. Get into underground formula buffering fill after the aluminium ash bale breaking, by the big inclination belt of buffering fill lower part carry get into the ball mill, ball mill feed inlet size 500mm sets up 2 storehouse structures, and grinding speed 5r/min, rinding body adopt 20cm and 2cm high strength zirconia ball, and the collection of big ball bobble is joined in marriage and is 1 storehouse: 4, 1,2 bins: 1:5. The angle of the guide vane of the discharge port dynamic powder concentrator is 30 degrees, and the rotor speed is 350rpm. A fines size D50=0.28mm was obtained. The coarse material discharged from the feed opening of the ball mill returns to the feed opening of the ball mill for further grinding.
The waste salt comes from a certain chemical area, and has 53.3% of chloride and 23.7% of carbon. The waste salt and the aluminum ash fine powder are fed into a double-shaft mixer to be mixed, and the proportion of the waste salt and the aluminum ash fine powder is 2:1. The mixed materials enter a reactor, the feeding amount is 1000kg/h, the chlorine concentration is 50%, the oxygen content is kept at 1.3%, the air pressure is 6000Pa, and the molten salt retention time is 30min. After the reaction, the flue gas enters a flue gas filtering chamber after heat is recovered by a waste heat boiler, the filtering temperature is 200 ℃, and powdery aluminum chloride is obtained, the yield is 1270kg/h, the purity is 94.2%, and the aluminum recovery rate reaches 96.7%. Molten salt enters a high-temperature filter chamber after reaction, residual chlorine in the flue gas after desulfurization and denitrification is introduced into the high-temperature filter chamber for preheating, and the chlorine flow is 25000m 3 H, the temperature of the flue gas outlet is 900 ℃. After the temperature of the molten salt is reduced, the solid material is suspended at the upper part of the molten salt and is discharged from an overflow port, and the yield of the recovered material is 54kg/h, wherein the content of ferric chloride is 70 percent, and the content of calcium chloride is 21 percent. And the molten salt discharged from the high-temperature filter chamber is pumped into the reactor again through a molten salt pump for recycling. The remaining molten salt was discharged into a stirred tank, mixed with water to form a brine, stirred for Chi Liusu 2.0.0 m/h, adjusted to pH8 with sodium hydroxide. The salt-containing water enters a desalting system to produce 306kg/h of sodium chloride and potassium chloride mixed salt with chloride content of 96 percent.
Example 3
The raw material aluminum ash is taken from a certain regenerated aluminum plant, the content of aluminum oxide is 45.3 percent, the content of metal aluminum is 2.8 percent, the content of ferric oxide is 3.2 percent, the content of calcium oxide is 4.7 percent, the content of nitride is 12.4 percent, the content of carbon is 0.2 percent, and the grain size D50=1.39mm. Get into underground formula buffering fill after the aluminium ash bale breaking, carry by the big inclination belt in buffering fill lower part and get into the ball mill, ball mill feed inlet size 400mm sets up 3 storehouse structures, and 8r/min of grinding speed, grinding body adopt 20cm and 2cm high strength zirconia ball, and big ball bobble collection is joined in marriage and is 1 storehouse: 4, 1,2 bins: 1, 5,3 bins: 1:5. The angle of the guide vane of the discharge port dynamic powder concentrator is 40 degrees, and the rotor speed is 250rpm. A fines size D50=0.41mm was obtained. The coarse material discharged from the feed opening of the ball mill returns to the feed opening of the ball mill for further grinding.
The waste salt comes from a certain chemical area, and has the sulfate content of 78.1 percent and the carbon content of 3.7 percent. The waste salt and the aluminum ash fine powder are fed into a double-shaft mixer to be mixed, and the proportion of the waste salt and the aluminum ash fine powder is 1:1. The mixed materials enter a reactor, the feeding amount is 1000kg/h, the chlorine concentration is 40 percent, the oxygen content is kept at 1 percent, the wind pressure is 9000Pa, the molten salt retention time is 60min, and the powdery sulfur is added as a deoxidizing and reducing agent. After the reaction, the flue gas enters a flue gas filtering chamber after heat is recovered by a waste heat boiler, the filtering temperature is 200 ℃, and powdery aluminum chloride is obtained, the yield is 1090kg/h, the purity is 97 percent, and the aluminum recovery rate reaches 95 percent. Molten salt enters a high-temperature filter chamber after reaction, residual chlorine in the flue gas after desulfurization and denitrification is introduced into the high-temperature filter chamber for preheating, and the chlorine flow is 40000m 3 H, the temperature of the flue gas outlet is 1000 ℃. After the temperature of the fused salt is reduced, the solid material is suspended at the upper part of the fused salt and is discharged from an overflow port, the yield of the recovered material is 52kg/h, wherein the content of ferric chloride is 40 percent, and the content of calcium chloride is 52 percent. And the molten salt discharged from the high-temperature filter chamber is pumped into the reactor again through a molten salt pump for recycling. The remaining molten salt was discharged into a stirred tank, mixed with water to form a brine, stirred for Chi Liusu 1.4.4 m/h, adjusted to pH8 with sodium hydroxide. The salt-containing water enters a desalting system to produce 309kg/h of sodium sulfate, sodium chloride and potassium chloride mixed salt, the chloride content is 13 percent, and the sulfate content is 86 percent.
In addition to the above embodiments, the present invention may have other embodiments. All technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope of the claims of the present invention.
Claims (9)
1. A method for recycling salt-containing solid waste is characterized by comprising the following steps: the method comprises the following steps:
(1) Grinding and selecting powder
Unpacking aluminum ash, conveying the aluminum ash into an underground buffer hopper from the lower part of the buffer hopper through a scale and a large-inclination-angle belt, conveying the aluminum ash into a grinding and powder selecting integrated system, grinding and synchronously selecting powder, then conveying fine particles into a material mixing and homogenizing system through the scale and a lifting machine, discharging coarse particles from the grinding system, and performing closed-loop circulation through the scale and a screw conveyor to enter the underground buffer hopper;
(2) Homogenizing mixed material
The fine particles in the step (1) enter a material mixing and homogenizing system, are fully homogenized with waste salt powder in a double-shaft mixer, and the homogenized fine particles are discharged from the lower part of the homogenizing system through a discharging machine and enter a reactor;
(3) Reductive chlorination
Feeding the homogenized material in the step (2) into molten salt from a feed inlet at the upper part of the reactor, blowing chlorine at the lower part of the reactor into a reaction chamber to react with the molten salt, discharging the reacted flue gas from the upper part of the reactor, and discharging the molten salt from the lower part of the reactor;
(4) Recovery of calcium and iron
In the step (3), the fused salt is mixed with chlorine blown into the bottom in the high-temperature filtering chamber, the cooled solid material is suspended at the upper part of the fused salt and is discharged from an overflow port, the calcium and iron material is recovered, the heated chlorine is discharged from the upper part of the filtering chamber and is blown into the reaction chamber, and the fused salt is returned to the reaction chamber by a fused salt pump;
(5) Recovering aluminium-containing material
Discharging the flue gas in the step (4), feeding the flue gas into a flue gas filtering chamber, separating aluminum chloride through a porous filtering pipe, feeding the separated flue gas into a rear-end desulfurization and denitrification treatment system, and returning the residual chlorine gas to the high-temperature filtering chamber for preheating;
(6) Salt recovery
And (4) discharging the excess molten salt in the system in the step (4) into a stirring tank, mixing the excess molten salt with water to form high-salt water, allowing the high-salt water to enter a salt recovery system, and crystallizing by using a triple-effect evaporator to obtain the sodium chloride potassium chloride salt mixed salt material.
2. The method for recycling solid waste containing salt according to claim 1, wherein the method comprises the following steps: in the step (1), a ball mill is adopted for grinding, the size of a feed inlet of the ball mill is 300-500mm, the ball mill is provided with a 2-3 bin structure, the grinding speed is 5-10r/min, a grinding body adopts 20cm and 5cm high-strength zirconia balls, and large balls and small balls are assembled into 1 bin: 1-4: 2:1-1:5, if 3 bins exist: 1:5-1:10.
3. The method for recycling solid waste containing salt according to claim 1, wherein the method comprises the following steps: in the step (1), a dynamic powder concentrator is adopted to select powder at a discharge port of the ball mill; the angle of the guide vane is 30-45 degrees, the rotor speed is 250-550rpm, and the size D50 of the obtained fine material is less than 0.5mm.
4. The method for recycling solid waste containing salt according to claim 1, wherein the method comprises the following steps: in the step (2), the ratio of the aluminum ash to the waste salt entering the double-shaft mixer is 4:1-1:1.
5. The method for recycling solid waste containing salt according to claim 1, wherein the method comprises the following steps: in the step (3), the reaction chamber is in the form of a molten salt furnace, and the highest refractory temperature is 1100 o C; the concentration of the chlorine gas is 50-20%, the balance gas is nitrogen, the oxygen content is less than 2%, the wind pressure is 5000-9000Pa, and the molten salt retention time is 30-60min; the deoxidation reducing agent is powdered carbon or sulfur.
6. The method for recycling the salt-containing solid waste as claimed in claim 1, wherein the method comprises the following steps: in the step (4), chlorine flow rate 10000-40000m is introduced into the high-temperature filter chamber 3 The temperature of the flue gas outlet is 900-1000 ℃.
7. The method for recycling solid waste containing salt according to claim 1, wherein the method comprises the following steps: in the step (5), a waste heat boiler is adopted to recover heat before the filtering chamber, the dusty smoke is filtered by a porous industrial ceramic tube, and the filtering temperature is 200-400 ℃.
8. The method for recycling solid waste containing salt according to claim 1, wherein the method comprises the following steps: in the step (6), the water flow speed of the stirring pool is 1.4-3.7m/h, and the pH value is adjusted to 7-8 by sodium hydroxide.
9. The method for recycling solid waste containing salt according to claim 1, wherein the method comprises the following steps: in the steps (1) - (6), air locking valves are installed at the solid material discharge ports to prevent gas leakage, the system connection adopts a closed device or a dust collector, and the system valve adopts an electric control valve and system interlocking function.
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|---|---|---|---|---|
| EP2274239A1 (en) * | 2008-05-13 | 2011-01-19 | Salt Extraction Aktiebolag | A process for chlorinating resources containing recoverable metals |
| CN102443710A (en) * | 2011-12-15 | 2012-05-09 | 沈阳化工大学 | Method for treating scrapped molten salt generated in molten salt chlorination production method of TiCl4 |
| CN103572323A (en) * | 2013-11-08 | 2014-02-12 | 中国科学院过程工程研究所 | Method for preparing aluminum silicon alloy through mixed chlorination and low-temperature electrolysis of aluminum-containing mineral and fly ash |
| CN106048226A (en) * | 2016-05-19 | 2016-10-26 | 东北大学 | Method for preparing metal aluminum through microwave chlorination of coal ash |
| CN110902706A (en) * | 2019-12-12 | 2020-03-24 | 东北大学 | Method for preparing polyaluminum chloride from aluminum ash |
| CN112718133A (en) * | 2020-12-17 | 2021-04-30 | 中信锦州金属股份有限公司 | Method and device for improving granularity of high-chromium low-iron vanadium fine slag |
-
2022
- 2022-09-14 CN CN202211114695.7A patent/CN115504494A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2274239A1 (en) * | 2008-05-13 | 2011-01-19 | Salt Extraction Aktiebolag | A process for chlorinating resources containing recoverable metals |
| CN102443710A (en) * | 2011-12-15 | 2012-05-09 | 沈阳化工大学 | Method for treating scrapped molten salt generated in molten salt chlorination production method of TiCl4 |
| CN103572323A (en) * | 2013-11-08 | 2014-02-12 | 中国科学院过程工程研究所 | Method for preparing aluminum silicon alloy through mixed chlorination and low-temperature electrolysis of aluminum-containing mineral and fly ash |
| CN106048226A (en) * | 2016-05-19 | 2016-10-26 | 东北大学 | Method for preparing metal aluminum through microwave chlorination of coal ash |
| CN110902706A (en) * | 2019-12-12 | 2020-03-24 | 东北大学 | Method for preparing polyaluminum chloride from aluminum ash |
| CN112718133A (en) * | 2020-12-17 | 2021-04-30 | 中信锦州金属股份有限公司 | Method and device for improving granularity of high-chromium low-iron vanadium fine slag |
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