CN115672931A - Recycling method of aluminum-containing solid waste - Google Patents
Recycling method of aluminum-containing solid waste Download PDFInfo
- Publication number
- CN115672931A CN115672931A CN202211115055.8A CN202211115055A CN115672931A CN 115672931 A CN115672931 A CN 115672931A CN 202211115055 A CN202211115055 A CN 202211115055A CN 115672931 A CN115672931 A CN 115672931A
- Authority
- CN
- China
- Prior art keywords
- aluminum
- solid waste
- containing solid
- recycling
- ash
- 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.)
- Pending
Links
Images
Classifications
-
- 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
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a method for recycling aluminum-containing solid waste, which relates to the technical field of solid waste treatment and comprises the following steps: the method comprises the following steps of grinding and powder selecting aluminum-containing solid waste, mixing and homogenizing the mixture, carrying out reduction chlorination, recycling calcium and iron, recycling aluminum-containing materials and recycling aluminum hydroxide, mixing aluminum ash and other aluminum-containing waste under the condition of no external heat by utilizing the characteristic that a large amount of heat is released in the chlorination process of AlN and Al metals in the reaction process of the aluminum ash and chlorine, converting aluminum in ash into aluminum chloride through reduction chlorination reaction, further reacting into high-purity aluminum hydroxide, improving the recycling value of the aluminum-containing ash, and realizing the comprehensive utilization of the green low-carbon aluminum-containing ash.
Description
Technical Field
The invention relates to the technical field of solid waste treatment, in particular to a method for recycling aluminum-containing solid waste.
Background
At present, the imported proportion of bauxite exceeds 50 percent in China, and aluminum resources are in urgent need of further recycling. The aluminum ash, the fly ash, the incineration fly ash and the like generate ash in the high-temperature process, the ash has high aluminum content, and the problem of shortage of aluminum resources can be well relieved. However, the utilization of the aluminum-containing ash has the following problems: (1) the reaction temperature of high-temperature sintering and the like is 1200-1400 ℃, a large amount of energy is needed for supporting, and the method is greatly limited under the control of a double-carbon target; (2) the ash contains more calcium and iron, a large amount of waste materials such as red mud are generated in the traditional chemical treatment process, and the problem of treatment of residues 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 aluminum-containing solid waste, which comprises the following steps:
(1) Grinding and selecting powder of aluminum-containing solid waste
Unpacking the aluminum-containing solid waste, conveying the aluminum-containing solid waste into an underground buffer hopper, conveying the aluminum-containing solid waste into a grinding and powder selecting integrated system through a metering scale and a large-inclination-angle belt on the lower part of the buffer hopper, grinding and synchronously selecting powder, conveying fine particles into a material mixing and homogenizing system through the metering scale and a lifting machine, discharging coarse particles from the grinding system, and conveying the coarse particles into the underground buffer hopper through the metering scale and a screw conveyer in a closed cycle manner;
(2) Homogenizing mixed material
The fine particles in the step (1) pass through a double-shaft mixer and then enter a mixing and homogenizing system for full homogenization, and the homogenized fine particles are discharged from a discharging machine at the lower part of the homogenizing system and enter a reactor;
(3) Reductive chlorination
Feeding the homogenized material in the step (2) from a feed inlet at the lower part of the reactor, mixing the homogenized material with blown chlorine at the lower part of the reactor, carrying the mixed material into a reaction chamber by the chlorine for reaction, discharging the reacted chloride material from the upper part of the reactor, and discharging and collecting the rest solid residues from the lower part of the reactor;
(4) Recovery of calcium and iron
The material-containing flue gas in the step (3) enters a precooling chamber at the upper part of the reactor, enters from the upper part at one side of the precooling chamber, is discharged from the upper part at the other side after being subjected to multiple baffling, and fine calcium chloride and iron chloride particles formed in the cooling process are settled to a collecting hopper at the lower part of the precooling chamber under the action of gravity and are discharged and recovered from the collecting hopper;
(5) Recovering aluminium-containing material
Enabling the flue gas discharged in the step (4) to enter a quench tower, absorbing the flue gas by cold water of the quench tower, enabling an aluminum-containing material and salt to be dissolved in water, discharging the flue gas out of the quench tower, enabling the flue gas to enter a sedimentation tank, enabling the flue gas after quenching to enter a rear-end desulfurization and denitrification treatment system through a gas-solid separator, and enabling residual chlorine to return to a reaction system;
(6) Recovery of aluminium hydroxide
The solution in the step (5) enters a sedimentation tank, pH adjustment is carried out, aluminum chloride is converted into aluminum hydroxide sediment and is discharged from the bottom of the sedimentation tank, and the aluminum hydroxide sediment is separated by a high-pressure filter press and then enters a dryer for drying to form a product; and discharging the solution after precipitation from an overflow groove of the precipitation tank, allowing the solution 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 invention further defines the technical scheme that:
in the foregoing method for recycling aluminum-containing solid waste, in step (1), one of the aluminum-containing solid waste is aluminum ash, the other one of the aluminum-containing solid waste is fly ash or waste incineration fly ash, and the aluminum-containing solid waste is ground and pulverized respectively.
In the method for recycling the aluminum-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, a 3-4 bin structure is arranged, the size of a grid hole of a partition plate is 15-25mm, the grinding speed is 10-15r/min, a grinding body adopts high-strength zirconia balls of 10cm and 2cm, and large balls and small balls are assembled into 1 bin: 12: 5:1-2: 1:2-1:8, if there are 4 bins: all the pellets.
In the method for recycling the aluminum-containing solid waste, in the step (1), a dynamic powder separator is adopted to perform powder separation at a discharge port of a ball mill, the angle of a guide vane is selected to be 30-45 degrees, the rotor speed is 350-650rpm, and the size D50 of the obtained fine material is less than 0.125mm.
In the foregoing method for recycling aluminum-containing solid waste, in the step (2), the ratio of the aluminum ash entering the mixer to other aluminum-containing solid waste is 10-3:1; the homogenizing system adopts a mode of arranging a small homogenizing chamber in a large storage bin, the volume ratio of the large storage bin to the small homogenizing chamber is 100-230, discharging is carried out for 5-15t/h, the homogenizing chamber adopts a screw machine for feeding, and a scraper plate for rotary discharging is adopted for discharging.
In the method for recycling the aluminum-containing solid waste, in the step (3), the reaction chamber is in the form of a vertical kiln, is lined with refractory materials, and has the highest refractory temperature of 1800 DEG C o C; the concentration of the chlorine gas is 80-30%, the balance gas is nitrogen gas, the oxygen content is less than 5%, and the flow rate is 20000-60000m 3 H, the retention time is 20-50min; the deoxidation reducing agent is powdered carbon or sulfur.
In the method for recycling the aluminum-containing solid waste, in the step (4), the pre-cooling chamber adopts a jacket structure, the temperature of the jacket is reduced by cold air, and the flow rate of heat exchange air is 5000-13000m 3 And h, the temperature of a flue gas outlet is 1000-1100 ℃, and air enters a dryer to dry the aluminum hydroxide product after heat exchange.
In the method for recycling the aluminum-containing solid waste, in the step (5), the quenching tower is sprayed by atomized water, and the temperature of flue gas at an outlet on the tower is 200-300 ℃.
In the method for recycling the aluminum-containing solid waste, in the step (6), the water flow speed of the sedimentation tank is 0.4-1.7m/h, the pH value is adjusted to 7-8 by sodium hydroxide, and the feeding pressure of the high-pressure filter press is 1.6-2.4 MPa.
In the method for recycling the aluminum-containing solid waste, in the steps (1) to (6), the air locking valves are arranged at the solid material discharge ports 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 a system.
The invention has the beneficial effects that:
(1) According to the invention, by utilizing 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, the aluminum ash is mixed with other aluminum-containing wastes under the condition of no external heat, aluminum in ash is converted into aluminum chloride through reduction chlorination reaction, and the aluminum chloride is further reacted into high-purity aluminum hydroxide, so that the resource utilization value of the aluminum-containing ash is improved, and the comprehensive utilization of green low-carbon aluminum-containing ash is realized;
(2) In the process, the incineration ash such as fly ash and waste incineration fly ash is added, and the carbon contained in the ash is utilized to catalyze the reduction of metal oxide and the generation of chloride thereof, so that the amount of an external carbon source is further reduced, and the full utilization of resources is realized;
(3) In the process of the invention, high-temperature chlorination converts stable ferric oxide and other impurities into ferric chloride, and separates iron impurities by using temperature-condensation effect, thereby realizing the purification of products;
(4) The invention adopts a multi-stage cooling mode to control the temperature in the process, can realize effective separation and collection of products at different temperature stages, and has no energy consumption. Meanwhile, high temperature generated by the system is subjected to heat exchange, waste heat is collected to dry products at each section, and the like, so that the self-heat-generation quantity of the system is fully utilized, the energy consumption of operation is further reduced, and the emission reduction of carbon dioxide is realized;
(5) The process of the invention can further purify the sodium chloride and the potassium chloride, improve the salt quality, reduce the cost of salt separation and generally realize the high value-added utilization of the aluminous ash.
Drawings
FIG. 1 is a schematic flow chart of the present invention.
Detailed Description
Example 1
The raw material 1 adopts aluminum ash of a certain regenerated aluminum plant in Zhejiang area of China, the content of aluminum oxide is 58.3%, the content of metal aluminum is 4.2%, the content of ferric oxide is 4.1%, the content of nitride is 15.8%, the content of carbon is 2.0%, and the particle size D50=0.45mm. 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 ball mill 1, 1 feed inlet size 300mm of ball mill sets up 3 storehouse structures, partition board comb hole size 25mm, and grinding speed 10r/min, the grinding body adopts 10cm and 2cm high strength zirconia ball, and big ball bobble collection is joined in marriage and is 1 storehouse: 8, 1,2 bins: 2, 1,3 bins: 1:8. The angle of the guide vane of the discharge port dynamic powder concentrator is selected to be 45 degrees, and the rotor speed is 650rpm. A fines size D50=0.93mm 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 raw material 2 adopts fly ash produced by a certain power plant in Zhejiang area of China, and has the content of aluminum oxide of 13.5 percent, the content of calcium oxide of 18.2 percent, the content of ferric oxide of 7.3 percent and the content of carbon of 3.8 percent. The raw material particle size D50=0.22mm. The coal ash enters an underground buffering hopper after unpacking, the coal ash is conveyed by a large-inclination-angle belt at the lower part of the buffering hopper to enter a ball mill 2, the size of a feed port of the ball mill 2 is 300mm, a 3-bin structure is arranged, the size of a grate hole of a bin separating plate is 15mm, the grinding speed is 10r/min, a grinding body adopts 10cm and 2cm high-strength zirconia balls, and a large ball and a small ball are assembled into 1 bin: 8, 1,2 bins: 2, 1,3 bins: 1:2. The angle of a guide vane of the discharge port dynamic powder concentrator is selected to be 30 degrees, the rotor speed is 350rpm, and the size D50=0.081mm of the fine material is 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.
Aluminium ash and fly ash are weighed through the spiral of taking the dashpot respectively and are sent into the compounding machine, and its proportion is 10, and the material is sent into big storage silo after the compounding, and wherein the volume ratio of big storage silo and little homogenization room is 230, and after abundant homogenization, the rotatory ejection of compact of scraper blade is adopted in the ejection of compact to 15t/h entering reaction chamber of load react. The chlorine concentration of the reaction is 80 percent, the oxygen content is kept at 4 percent, and the flow rate is 60000m 3 H, residence time 20min. The reaction does not require powdered carbon make-up. After the reaction, the output of the discharged slag at the lower part of the reactor is 3.3t/h, wherein the content of silicon oxide is 54 percent, the content of calcium oxide is 3.2 percent, the content of ferric oxide is 1.1 percent, the content of chloride is 0.04 percent, and the content of nitride is 0.01 percent, and the slag can be used as an admixture of building materials. The flue gas after reaction enters a pre-cooling chamber for heat exchange, and the air flow is 13000m 3 And h, the temperature of a flue gas outlet is 1100 ℃. Calcium chloride and ferric chloride fine particles formed by cooling in the pre-cooling chamber enter a collecting hopper to be collected and recycled, the product yield is 1.1t/h, and the content of ferric chloride is 55% and the content of calcium chloride is 44%. Spraying atomized water after the flue gas at the outlet of the precooling chamber enters a quench tower, absorbing the flue gas at the outlet of the precooling chamber by cold water of the quench tower, discharging an aluminum-containing material and salt dissolved in water out of the quench tower, feeding the aluminum-containing material and the salt into a sedimentation tank, adjusting the pH value of the sedimentation tank to be 8 by using sodium hydroxide, dehydrating the material by using a high-pressure filter press, drying a wet filter cake under the feeding pressure of 1.6 MPa to obtain the product of the aluminum hydroxide with the yield of 11.2t/h (the purity is 98.3 percent in terms of aluminum oxide)The Al recovery (based on alumina) was 94.5%. The filtrate is evaporated to obtain the potassium-sodium mixed chloride salt with the yield of 1.4t/h and the sodium chloride content of 95 percent.
Example 2
The raw material 1 is aluminum ash of a certain regenerated aluminum plant in Shandong area of China, the content of aluminum oxide is 48.2%, the content of metal aluminum is 3.1%, the content of ferric oxide is 8.6%, the content of nitride is 20.4%, the content of carbon is 1.0%, and the particle size D50=1.8mm. 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 ball mill 1, 1 feed inlet size 500mm of ball mill sets up 4 storehouse structures, partition board comb hole size 15mm, and grinding speed 15r/min, the grinding body adopts 10cm and 2cm high strength zirconia ball, and big ball bobble collection is joined in marriage and is 1 storehouse: 10, 1,2 bins: 5, 1,3 bins: 1:2, if there are 4 bins: all the pellets. The angle of the guide vane of the discharge port dynamic powder concentrator is selected to be 45 degrees, and the rotor speed is 450rpm. A fines size D50=0.076mm 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 raw material 2 is fly ash produced by a power plant in Shandong area of China, and has the content of aluminum oxide of 10.1 percent, the content of calcium oxide of 22.1 percent, the content of ferric oxide of 4.3 percent and the content of carbon of 5.2 percent. The raw material particle size D50=0.29mm. The coal ash enters an underground buffering hopper after being unpacked, the coal ash is conveyed by a large-inclination-angle belt at the lower part of the buffering hopper to enter a ball mill 2, the size of a feed inlet of the ball mill 2 is 300mm, a 3-bin structure is arranged, the size of a grate hole of a partition plate is 15mm, the grinding rotating speed is 15r/min, a grinding body adopts 10cm and 2cm high-strength zirconia balls, and large balls and small balls are assembled into 1 bin: 9, 1,2 bins: 3, 1,3 bins: 1:6. The angle of the guide vane of the discharge port dynamic powder concentrator is selected to be 30 degrees, the rotor speed is 650rpm, and the size D50=0.062mm of the fine material is 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 aluminum ash and the fly ash are respectively fed into the mixer through a spiral weighing scale with a buffer tank, the proportion of the aluminum ash and the fly ash is 8:1, the mixed materials are fed into a large storage bin, the volume ratio of the large storage bin to a small homogenizing chamber is 100, after full homogenization, the discharged materials are discharged by adopting a scraper to rotate, and the discharged materials enter a reaction chamber for reaction at the discharge amount of 5 t/h. The concentration of the chlorine gas in the reaction is 30 percent, the oxygen content is kept at 2 percent, and the flow rate is 20000m 3 H, residence time 50min is the same as the formula (I). The reaction does not require powdered carbon make-up. After the reaction, the output of the discharged slag at the lower part of the reactor is 1.4t/h, wherein the content of silicon oxide is 67 percent, the content of calcium oxide is 7.7 percent, the content of ferric oxide is 1.0 percent, the content of chloride is 0.02 percent, and the content of nitride is 0.03 percent, and the discharged slag can be used as a building material admixture. The flue gas after reaction enters a pre-cooling chamber for heat exchange, and the air flow is 5000m 3 The temperature of the flue gas outlet is 1000 ℃. Calcium chloride and ferric chloride fine particles formed by cooling in the pre-cooling chamber enter a collecting hopper to be collected and recycled, the product yield is 0.6t/h, the ferric chloride content is 64 percent, and the calcium chloride content is 35 percent. The flue gas at the outlet of the pre-cooling chamber enters a quench tower and is sprayed by atomized water, the temperature of the flue gas at the outlet of the tower is 200 ℃, after the flue gas is absorbed by cold water of the quench tower, an aluminum-containing material and salt are dissolved in water and are discharged out of the quench tower, the flue gas enters a sedimentation tank, the water flow speed of the sedimentation tank is 1.0m/h, the pH value is adjusted by sodium hydroxide to be 8, the material is dehydrated by a high-pressure filter press, the feeding pressure is 1.6 MPa, a wet filter cake is dried, the yield of an aluminum hydroxide product is 3.3t/h (the purity is 99.3 percent in terms of aluminum oxide), and the recovery rate of Al (in terms of aluminum oxide) is 93 percent. The filtrate is evaporated to obtain the potassium-sodium mixed chloride salt with the yield of 0.44t/h and the sodium chloride content of 96 percent.
Example 3
The raw material 1 is aluminum ash of a certain recycled aluminum plant in Jiangsu area of China, the content of aluminum oxide is 63.1%, the content of metal aluminum is 5.0%, the content of ferric oxide is 5.3%, the content of nitride is 12.6%, the content of carbon is 0.6%, and the particle size D50=3.3mm. 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 ball mill 1, 1 feed inlet size 500mm of ball mill sets up 4 storehouse structures, partition board comb hole size 15mm, and grinding speed 10r/min, the grinding body adopts 10cm and 2cm high strength zirconia ball, and big ball bobble collection is joined in marriage and is 1 storehouse: 12, 1,2 bins: 3, 1,3 bins: 1:8, if there are 4 bins: all the pellets. The angle of the guide vane of the discharge port dynamic powder concentrator is 40 degrees, and the rotor speed is 650rpm. A fines size D50=0.118mm was obtained. And returning the coarse material discharged from the feed opening of the ball mill to the feed opening of the ball mill for further grinding.
The raw material 2 adopts fly ash produced by a certain waste incineration plant in Jiangsu areas of China, and has the aluminum oxide content of 7.4 percent, the calcium oxide content of 34.8 percent, the ferric oxide content of 11.2 percent and the carbon content of 1.9 percent. The raw material particle size D50=0.14mm. The coal ash enters an underground buffering hopper after being unpacked, the coal ash is conveyed by a large-inclination-angle belt at the lower part of the buffering hopper to enter a ball mill 2, the size of a feed inlet of the ball mill 2 is 300mm, a 3-bin structure is arranged, the size of a grate hole of a partition plate is 25mm, the grinding rotating speed is 15r/min, a grinding body adopts 10cm and 2cm high-strength zirconia balls, and large balls and small balls are assembled into 1 bin: 8, 1,2 bins: 5, 1,3 bins: 1:8. And selecting the angle of a guide vane of the dynamic powder concentrator at the discharge port to be 45 degrees, and rotating at the speed of 650rpm to obtain the fine material D50=0.036mm. 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 aluminum ash and the fly ash are respectively fed into the mixer through a spiral weighing scale with a buffer tank, the proportion of the aluminum ash and the fly ash is 3:1, the mixed materials are fed into a large storage bin, the volume ratio of the large storage bin to a small homogenizing chamber is 150, after sufficient homogenization, the discharged materials are discharged by adopting a scraper to rotate, and the discharged materials enter a reaction chamber for reaction at the discharge amount of 10 t/h. The concentration of the chlorine gas in the reaction is 50 percent, the oxygen content is kept at 2 percent, and the flow rate is 40000m 3 H, residence time 40min. The reaction replenishes the powdered carbon to catalyze the metal chloride generation. After the reaction, the output of the discharged slag at the lower part of the reactor is 1.6t/h, wherein the content of silicon oxide is 59 percent, the content of calcium oxide is 6.5 percent, the content of ferric oxide is 0.6 percent, the content of chloride is 0.01 percent, and the content of nitride is 0.02 percent, thus the slag can be used as an admixture of building materials. The flue gas after reaction enters a pre-cooling chamber for heat exchange, and the air flow is 12000m 3 The temperature of the flue gas outlet is 1000 ℃. Calcium chloride and ferric chloride fine particles formed by cooling in the pre-cooling chamber enter a collecting hopper to be collected and recycled, the product yield is 1.5t/h, and the content of ferric chloride is 32 percent and the content of calcium chloride is 67 percent. The flue gas at the outlet of the pre-cooling chamber enters a quench tower and is sprayed by atomized water, the temperature of the flue gas at the outlet of the tower is 200 ℃, after the flue gas is absorbed by cold water of the quench tower, an aluminum-containing material and salt are dissolved in water and are discharged out of the quench tower, the flue gas enters a sedimentation tank, the water flow speed of the sedimentation tank is 1.7m/h, the pH value is adjusted by sodium hydroxide to be 7, the material is dehydrated by a high-pressure filter press, the feeding pressure is 2.4 MPa, a wet filter cake is dried, the yield of an aluminum hydroxide product is 6.7t/h (calculated by aluminum oxide, the purity is 98.1%), and the Al recovery rate (calculated by aluminum oxide) is 98%. The filtrate is evaporated to obtain the potassium-sodium mixed chloride salt with the yield of 1.38t/h and the sodium chloride content of 93 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 (10)
1. A method for recycling aluminum-containing solid waste is characterized by comprising the following steps: the method comprises the following steps:
(1) Grinding and selecting powder of aluminum-containing solid waste
Unpacking the aluminum-containing solid waste, conveying the aluminum-containing solid waste into an underground buffer hopper, conveying the aluminum-containing solid waste into a grinding and powder selecting integrated system through a metering scale and a large-inclination-angle belt on the lower part of the buffer hopper, grinding and synchronously selecting powder, conveying fine particles into a material mixing and homogenizing system through the metering scale and a lifting machine, discharging coarse particles from the grinding system, and conveying the coarse particles into the underground buffer hopper through the metering scale and a screw conveyer in a closed cycle manner;
(2) Homogenizing mixed material
The fine particles in the step (1) pass through a double-shaft mixer and then enter a mixing and homogenizing system for full homogenization, and the homogenized fine particles are discharged from a discharging machine at the lower part of the homogenizing system and enter a reactor;
(3) Reductive chlorination
Feeding the homogenized material in the step (2) from a feed inlet at the lower part of the reactor, mixing the homogenized material with the blown chlorine at the lower part of the reactor, carrying the chlorine into a reaction chamber for reaction, discharging the reacted chloride material from the upper part of the reactor, and discharging and collecting the rest solid residues from the lower part of the reactor;
(4) Recovery of calcium and iron
The material-containing flue gas in the step (3) enters a precooling chamber at the upper part of the reactor, enters from the upper part at one side of the precooling chamber, is discharged from the upper part at the other side after being subjected to multiple baffling, and fine calcium chloride and iron chloride particles formed in the cooling process are settled to a collecting hopper at the lower part of the precooling chamber under the action of gravity and are discharged and recovered from the collecting hopper;
(5) Recovering aluminium-containing material
Allowing the flue gas discharged in the step (4) to enter a quench tower, absorbing the flue gas by cold water in the quench tower, dissolving an aluminum-containing material and salt in water, discharging the flue gas out of the quench tower, allowing the flue gas to enter a sedimentation tank, allowing the flue gas subjected to quenching to enter a rear-end desulfurization and denitrification treatment system through a gas-solid separator, and returning the residual chlorine to a reaction system;
(6) Recovery of aluminium hydroxide
The solution in the step (5) enters a sedimentation tank, pH adjustment is carried out, aluminum chloride is converted into aluminum hydroxide sediment and is discharged from the bottom of the sedimentation tank, and the aluminum hydroxide sediment is separated by a high-pressure filter press and then enters a dryer for drying to form a product; and discharging the precipitated solution from an overflow groove of the precipitation tank, allowing the solution to enter a salt recovery system, and crystallizing by using a triple-effect evaporator to obtain a sodium chloride potassium chloride salt mixed salt material.
2. The method for recycling the aluminum-containing solid waste as claimed in claim 1, wherein the method comprises the following steps: in the step (1), one of the aluminum-containing solid wastes is aluminum ash, the other one of the aluminum-containing solid wastes is fly ash or waste incineration fly ash, and the aluminum-containing solid wastes are respectively ground and subjected to powder selection.
3. The method for recycling the aluminum-containing solid waste as claimed in 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, a 3-4 bin structure is arranged, the size of a grid hole of a partition plate is 15-25mm, the grinding speed is 10-15r/min, a grinding body adopts 10cm and 2cm high-strength zirconia balls, and large balls and small balls are assembled into 1 bin: 12: 5:1-2: 1:2-1:8, if there are 4 bins: all the pellets.
4. The method for recycling aluminum-containing solid waste as claimed in claim 1, wherein: in the step (1), a dynamic powder selecting machine is adopted to select powder at a discharge port of the ball mill, the angle of a guide vane is 30-45 degrees, the speed of a rotor is 350-650rpm, and the size D50 of the obtained fine material is less than 0.125mm.
5. The method for recycling the aluminum-containing solid waste as claimed in claim 1, wherein the method comprises the following steps: in the step (2), the ratio of the aluminum ash entering the mixer to other aluminum-containing solid waste is 10-3:1; the homogenizing system adopts a mode of arranging a small homogenizing chamber in a large storage bin, the volume ratio of the large storage bin to the small homogenizing chamber is 100-230, discharging is carried out for 5-15t/h, the homogenizing chamber adopts a screw machine for feeding, and a scraper plate for rotary discharging is adopted for discharging.
6. The method for recycling the aluminum-containing solid waste as claimed in claim 1, wherein the method comprises the following steps: in the step (3), the reaction chamber is in the form of a vertical kiln, is lined with refractory materials and has the highest refractory temperature of 1800 DEG C o C; the concentration of the chlorine gas is 80-30%, the balance gas is nitrogen gas, the oxygen content is less than 5%, and the flow rate is 20000-60000m 3 The residence time is 20-50min; the deoxidation reducing agent is powdered carbon or sulfur.
7. The method for recycling the aluminum-containing solid waste as claimed in claim 1, wherein the method comprises the following steps: in the step (4), the pre-cooling chamber adopts a jacket structure, the temperature of the jacket is reduced by cold air, and the flow of heat exchange air is 5000-13000m 3 And h, the temperature of a flue gas outlet is 1000-1100 ℃, and air enters a dryer to dry the aluminum hydroxide product after heat exchange.
8. The method for recycling the aluminum-containing solid waste as claimed in claim 1, wherein the method comprises the following steps: in the step (5), the quenching tower adopts atomized water for spraying, and the temperature of the flue gas at the upper outlet of the tower is 200-300 ℃.
9. The method for recycling the aluminum-containing solid waste as claimed in claim 1, wherein the method comprises the following steps: in the step (6), the water flow speed of the sedimentation tank is 0.4-1.7m/h, the pH value is adjusted to 7-8 by sodium hydroxide, and the feeding pressure of the high-pressure filter press is 1.6-2.4 MPa.
10. The method for recycling the aluminum-containing solid waste as claimed in 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 valves adopt an electric control valve and system interlocking function.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211115055.8A CN115672931A (en) | 2022-09-14 | 2022-09-14 | Recycling method of aluminum-containing solid waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211115055.8A CN115672931A (en) | 2022-09-14 | 2022-09-14 | Recycling method of aluminum-containing solid waste |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115672931A true CN115672931A (en) | 2023-02-03 |
Family
ID=85062031
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211115055.8A Pending CN115672931A (en) | 2022-09-14 | 2022-09-14 | Recycling method of aluminum-containing solid waste |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115672931A (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102249253A (en) * | 2011-01-06 | 2011-11-23 | 内蒙古大唐国际再生资源开发有限公司 | Method for producing aluminum oxide and co-producing active calcium silicate through high-alumina fly ash |
| CN102491394A (en) * | 2011-11-22 | 2012-06-13 | 中国铝业股份有限公司 | Method for producing aluminum chloride by using fly ash |
| CN102502665A (en) * | 2011-11-22 | 2012-06-20 | 中国铝业股份有限公司 | Method for comprehensively recovering valuable elements in coal ash |
| CN102644093A (en) * | 2011-02-16 | 2012-08-22 | 贵阳铝镁设计研究院有限公司 | Method for producing metal aluminium by high-alumina fly ash chlorination electrolysis |
| 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 CN202211115055.8A patent/CN115672931A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102249253A (en) * | 2011-01-06 | 2011-11-23 | 内蒙古大唐国际再生资源开发有限公司 | Method for producing aluminum oxide and co-producing active calcium silicate through high-alumina fly ash |
| CN102644093A (en) * | 2011-02-16 | 2012-08-22 | 贵阳铝镁设计研究院有限公司 | Method for producing metal aluminium by high-alumina fly ash chlorination electrolysis |
| CN102491394A (en) * | 2011-11-22 | 2012-06-13 | 中国铝业股份有限公司 | Method for producing aluminum chloride by using fly ash |
| CN102502665A (en) * | 2011-11-22 | 2012-06-20 | 中国铝业股份有限公司 | Method for comprehensively recovering valuable elements in coal ash |
| 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 |
Non-Patent Citations (1)
| Title |
|---|
| 邱竹贤: "铝电解", 铝电解, pages: 238 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US11286162B2 (en) | System and method for recovering sulfur in copper smelting process | |
| CN109809456B (en) | System and method for co-producing calcium oxide and sulfur by coal gasification and gypsum calcination | |
| CN110803877B (en) | Device and method for producing II-type anhydrous gypsum from desulfurized gypsum | |
| CN108503247B (en) | Method and equipment for producing high-temperature gypsum from industrial byproduct gypsum | |
| CN113247932A (en) | System for preparing polyaluminum chloride from aluminum ash and manufacturing method of polyaluminum chloride | |
| CN104211030A (en) | Improved method using rotary kiln for large scale production of phosphoric acid | |
| CN106927699A (en) | A kind of method that utilization carbide slag prepares calcium carbide lime | |
| US20170088467A1 (en) | Apparatus and Method for Producing Cement Through Flue Gas Desulfurization | |
| CN108585564B (en) | System and method for co-processing electrolytic aluminum waste residues and co-producing double quick cement by cement kiln | |
| CN112520769B (en) | Process and device for dealkalizing red mud and simultaneously recovering aluminum oxide by using waste flue gas and waste heat of cement plant | |
| CN101955166B (en) | Method for decomposing semi-hydrated phosphogypsum | |
| CN108046302A (en) | A kind of method that carbide slag produces high-purity white lime | |
| CN109108050B (en) | Method and system for converting sodium-containing and fluorine-containing compounds in aluminum electrolysis overhaul residues | |
| CN101497939B (en) | Novel method for producing iron ore pellet binder | |
| CN115672931A (en) | Recycling method of aluminum-containing solid waste | |
| CN106006643A (en) | Method for preparing calcium carbide from yellow phosphorus tail gas and phosphogypsum | |
| CN210945395U (en) | Device for producing II type anhydrous gypsum from desulfurized gypsum | |
| CN212610834U (en) | High-sulfur bauxite dry-process desulfurization device | |
| CN1243687C (en) | Method for producing phosphoric acid and cement from phosphate ore by hot process | |
| CN211799379U (en) | Coal vertical mill dust settling system for drying pulverized coal by using waste gas of kiln head of cement kiln | |
| CN112811448A (en) | Recovery process of magnesium oxide reducing slag | |
| CN113751214A (en) | System and process for resourcefully treating waste incineration fly ash | |
| CN215479774U (en) | System for aluminium ash preparation polyaluminium chloride | |
| CN111621639A (en) | High-sulfur bauxite dry-process desulfurization device and method | |
| CN113955791A (en) | Comprehensive utilization method of household garbage incineration fly ash |
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 |