Secondary aluminum ash treatment device and treatment method

Abstract

The present disclosure relates to a secondary aluminum ash treatment device which includes a storage tank, a heating reaction means, and a heat-retention reaction means which are connected in series, the storage tank is provided with a supply port for supplying aluminum ash, the heating reaction means includes n heating reaction tanks which are respectively a first class heating reaction tank, a second class heating reaction tank, ... an nth class heating reaction tank and connected in series, each of the n heating reaction tanks is provided with a first exhaust port for discharging gas, and the heat-retention reaction means includes m heating reaction tanks which are respectively a first class heating reaction tank, a second class heating reaction tank, ... an mth class heating reaction tank and connected in series, each of the m heating reaction tanks is provided with a second exhaust port for discharging gas.

Description

[Technical Field]

[0001] <Cross-citation of related applications> This application claims priority from a Chinese patent application filed on November 28, 2022, bearing application number 202211505167.4, the entire contents of which are incorporated herein by reference. [Background technology]

[0002] The present disclosure relates to the aluminum industry, and more particularly to a device and method for treating secondary aluminum ash. Summary of the Invention [Problem to be solved by the invention]

[0003] In recent years, as aluminum consumption has increased, the output of aluminum processing has also increased. Energy shortages and environmental pressures have placed constraints and restrictions on the high-energy production of virgin aluminum. The aluminum scrap recycling industry is undergoing upgrading and development, resulting in a gradual increase in aluminum ash output. Aluminum ash is a solid hazardous waste product generated during aluminum production. It can be divided into primary and secondary aluminum ash depending on its metallic aluminum content. Aluminum ash discharged into blast furnaces is also known as "primary aluminum ash" or "white aluminum ash." Secondary aluminum ash is the aluminum ash generated after metallic aluminum is extracted from primary aluminum ash. In secondary aluminum ash, the main aluminum-containing substances are Al2O3, AlN, Al, MgAl2O4, Al4C3, etc., the main chloride salt substances are NaCl, KCl, etc., the fluorine-containing substances are CaF2, Na3AlF6, etc., and it also contains small amounts of oxides such as SiO2 and Fe2O3. Secondary aluminum ash contains AlN, elemental Al, fluorides, etc., making it reactive and toxic. It was included in the National Catalog of Hazardous Wastes (2021 Edition) in 2021, and its use and handling must comply with hazardous waste standards.

[0004] Conventional secondary aluminum ash treatment methods primarily rely on a single intermittent reaction system to solve the problem of "single intermittent reaction" of secondary aluminum ash. That is, secondary aluminum ash is intermittently reacted in the same reaction space. When secondary aluminum ash is treated with a single intermittent reaction, the active components in secondary aluminum ash are primarily AlN, elemental Al, and Al4C3 at different reaction stages. Because the degree and reaction rate of AlN, elemental Al, and Al4C3 vary, the gas generation rate and amount of gas produced vary at different stages during the reaction of secondary aluminum ash. This results in significant gas generation backlash and makes the reaction rate difficult to control. In other words, as the reaction of secondary aluminum ash progresses, the state of the reaction system changes rapidly, making it difficult to control. Therefore, a single intermittent reaction makes it difficult to operate stably. [Means for solving the problem]

[0005] One or more embodiments using the teachings of the present disclosure can solve the technical problem of the difficulty of stably operating a single intermittent reaction.

[0006] According to a first aspect of the present disclosure, there is provided a secondary aluminum ash treatment device, which includes a storage tank, a temperature-raising reaction means, and a heat-retention reaction means, which are sequentially connected to one another. The storage tank is equipped with a supply port for supplying aluminum ash. The temperature-raising reaction means includes n temperature-raising reaction tanks connected in series, each of which is a first-class temperature-raising reaction tank, a second-class temperature-raising reaction tank, ... an n-th class temperature-raising reaction tank. Each of the n temperature-raising reaction tanks connected in series is equipped with a first exhaust port for discharging gas. The heat-retention reaction means includes m temperature-raising reaction tanks connected in series, each of which is a first-class temperature-raising reaction tank, a second-class temperature-raising reaction tank, ... an m-th class temperature-raising reaction tank. Each of the m temperature-raising reaction tanks connected in series is equipped with a second exhaust port for discharging gas.

[0007] According to a second aspect of the present disclosure, there is provided a method for treating secondary aluminum ash, the method for treating secondary aluminum ash comprising the steps of: providing a secondary aluminum ash treatment device according to any one of the embodiments of the first aspect; supplying secondary aluminum ash and water from the supply port to the storage tank to form a first slurry in the storage tank; guiding the slurry to a first temperature-raised reaction tank and supplying a stabilizer to the first temperature-raised reaction tank to promote hydrolysis of elemental Al and Al4C3 while suppressing hydrolysis of AlN to form a second slurry; allowing the second slurry to flow from the first temperature-raised reaction tank to an n-th temperature-raised reaction tank to form a third slurry in the n-th temperature-raised reaction tank; and discharging a gaseous stream generated by the reaction from the first temperature-raised reaction tank to the n-th temperature-raised reaction tank. the fourth slurry flows from the first-class heat-insulating reaction tank to the n-class heat-insulating reaction tank, and a dechlorinating agent is supplied to the n-class heat-insulating reaction tank to increase the particle size of the solid particles and promote the precipitation of salt substances; the dechlorinating agent and the fourth slurry are mixed and reacted to form a fifth slurry, and gas generated by the reaction in the first to n-class heat-insulating reaction tanks is collected; and the fifth slurry is filtered to obtain a filtrate, and the filtrate is concentrated and crystallized. [Brief explanation of the drawings]

[0008] The drawings herein are incorporated into and constitute a part of this specification, illustrate embodiments consistent with the present disclosure, and together with the specification, serve to interpret the spirit and scope of the present disclosure.

[0009] In order to more clearly explain the technical means in the embodiments or prior art of the present disclosure, the following briefly introduces drawings necessary for the description of the embodiments or prior art, but it is obvious that those skilled in the art can obtain other drawings based on these drawings as long as there is no work worth the inventive step.

[0010] [Figure 1] Schematic diagram showing the configuration of a secondary aluminum ash treatment device according to some embodiments of the present disclosure. DETAILED DESCRIPTION OF THE INVENTION

[0011] In order to clarify the purpose, technical means and advantages of the embodiments of the present disclosure, the technical means in the embodiments of the present disclosure will be clearly and completely described below with reference to the drawings in the embodiments of the present disclosure. It is clear that the described embodiments are only a part of the embodiments of the present disclosure, and are not all of the embodiments. All other embodiments that can be made based on the embodiments of the present disclosure without the work of a person skilled in the art that does not add an inventive step are all within the scope of protection of the present disclosure.

[0012] Unless otherwise specified, terms used herein should be understood as commonly used in the art. Therefore, unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the art. In the event of a conflict, the present specification shall prevail.

[0013] Unless otherwise specified, each raw material, reagent, instrument, or device used in this disclosure is commercially available or can be produced by conventional methods.

[0014] Conventional secondary aluminum ash treatment devices and methods have the technical problem of difficulty in stable operation due to a single intermittent reaction. The technical means provided in the embodiments of the present disclosure solve the above technical problem through the following overall concept:

[0015] The first aspect is shown in FIG. 1. The secondary aluminum ash treatment device provided by the embodiment of the present disclosure includes a storage tank, a temperature-raising reaction means, and a heat-retention reaction means, which are sequentially connected to one another. The storage tank is equipped with a supply port for supplying secondary aluminum ash. The temperature-raising reaction means includes n temperature-raising reaction tanks connected in series, each of which is a first-class temperature-raising reaction tank, a second-class temperature-raising reaction tank, and so on, up to an nth-class temperature-raising reaction tank. Each of the n temperature-raising reaction tanks connected in series is equipped with a first exhaust port for discharging gas. The heat-retention reaction means includes m temperature-raising reaction tanks connected in series, each of which is a first-class temperature-raising reaction tank, a second-class temperature-raising reaction tank, and so on, up to an mth-class temperature-raising reaction tank. Each of the m temperature-raising reaction tanks connected in series is equipped with a second exhaust port for discharging gas.

[0016] The storage tank is used to mix the raw materials, and the process of mixing the raw materials involves uniformly mixing the secondary aluminum ash and water. The storage tank is equipped with a device for uniformly mixing the secondary aluminum ash and water. This device is a device commonly found in this field, and may be, for example, a mixing paddle or a mixing screw.

[0017] As the reaction between secondary aluminum ash and water progresses, the state of the reaction system constantly changes. By installing n heating reaction tanks and m heat-retaining reaction tanks, the reaction system at different reaction stages can be controlled in different tank bodies.

[0018] The active components of secondary aluminum ash at different reaction stages are mainly AlN, elemental Al, and Al4C3, and the reaction degree and reaction rate of AlN, elemental Al, and Al4C3 are different. Among them, elemental Al and Al4C3 have relatively high reactivity and mainly react in the temperature-raising reaction means to generate combustible gases including hydrogen and hydrocarbons. AlN mainly reacts in the temperature-retaining reaction means to generate ammonia.

[0019] The present disclosure provides a system for treating secondary aluminum ash by installing multiple temperature-raising reaction tanks connected in series with each other and multiple heat-retaining reaction tanks connected in series with each other, allowing different reaction systems with different reaction stages to react in different tank bodies, making it easy to control the progress of the reactions. The reaction of elemental Al and Al4C3 occurs primarily within the temperature-raising reaction means, while the reaction of AlN occurs primarily within the heat-retaining reaction means, allowing the generated combustible gas and ammonia to be easily collected. Furthermore, the secondary aluminum ash treatment system according to the present disclosure has a simple configuration and can be easily implemented on a large scale.

[0020] In some embodiments of the present disclosure, n is 0.45+58×X−260×X 2 The result of the above calculation is rounded off to the nearest integer, where X=A+B, where A is the mass ratio of elemental aluminum to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash.

[0021] The process for obtaining the above equation is as follows. For secondary aluminum ash with different contents of elemental Al, Al4C3, and AlN, continuous reaction tests are conducted using reaction tanks connected in series to obtain multiple sets of systematic data for the hydrolysis of secondary aluminum ash. Each set of data has the same X and variable n. By monitoring the reaction progress, an n value that promotes the full reaction between Al and Al4C3 while suppressing the reaction of AlN is found. Since the X values ​​vary for different data sets, a series of X and n values ​​that promote the full reaction between Al and Al4C3 can be obtained. Observation reveals that the linear relationship between n and X is relatively poor. As X increases, n tends to increase rapidly first, then gradually. Therefore, a quadratic equation provides a relatively good fit. Therefore, the relationship between X and the number of heating reaction tanks, n, conforms to a quadratic equation, and the above equation is obtained by numerical simulation.

[0022] In some embodiments of the present disclosure, m is an integer obtained by rounding off the result calculated using the formula 22 × Z + 1.2, where Z is the mass ratio of AlN to secondary aluminum ash.

[0023] The process for obtaining the above formula is as follows: For secondary aluminum ash with different contents of elemental Al, Al4C3, and AlN, continuous reaction tests are conducted using a continuous reaction tank to obtain multiple systematic data sets for the hydrolysis of secondary aluminum ash, with the same Z and variable m. By monitoring the progress of the reaction, the m value at which AlN is fully hydrolyzed is determined. Since the Z values ​​vary for different data sets, a series of Z and m values ​​useful for fully hydrolyzing AlN can be obtained. Observations show that the linear relationship between m and Z is relatively good. Therefore, a linear equation is applied, and the fitting results are relatively good. Therefore, in this disclosure, the relationship between the mass ratio Z of AlN to aluminum ash and the number m of heat-insulating reaction tank bodies conforms to a linear equation, and as Z increases, m tends to increase linearly. Therefore, the above formula is calculated and obtained through numerical simulation.

[0024] According to a second aspect, an embodiment of the present disclosure provides a method for treating secondary aluminum ash, the method comprising the steps of: Step S1 provides a secondary aluminum ash treatment device according to any one of the embodiments in the first aspect. Step S2 supplies secondary aluminum ash and water from a supply port into a storage tank to form a first slurry in the storage tank. In step S3, while guiding the first slurry to a primary heating reaction tank, a stabilizer is supplied into the primary heating reaction tank to promote hydrolysis of elemental Al and Al4C3 while suppressing the hydrolysis of AlN, thereby forming a second slurry. In step S4, the second slurry is caused to flow from the first temperature-raised reaction tank to the nth temperature-raised reaction tank, a third slurry is formed in the nth temperature-raised reaction tank, and gas generated by the reaction in the first temperature-raised reaction tank to the nth temperature-raised reaction tank is collected. In step S5, while guiding the third slurry to the first heat-retaining reaction tank, an activator for increasing the hydrolysis activity of AlN is supplied to the first heat-retaining reaction tank to form a fourth slurry. In step S6, the fourth slurry flows from the first-class heat-retaining reaction tank to the n-class heat-retaining reaction tank, a dechlorinating agent is supplied to the n-class heat-retaining reaction tank to increase the particle size of solid particles and promote the precipitation of salt substances, the dechlorinating agent and the fourth slurry are mixed and reacted to form a fifth slurry, the gas generated by the reaction in the first-class heat-retaining reaction tank to the n-class heat-retaining reaction tank is collected, the fifth slurry is filtered to obtain a filtrate, and the filtrate is concentrated and crystallized.

[0025] Those skilled in the art can understand that the liquid phase always exists in the form of a slurry during the reaction, and the slurry can be systematically powered by a common method commonly seen in this field to gradually guide the slurry from the storage tank to the n-level heat-retaining reaction tank. For example, the method of powering the slurry can be to add a liquid pump and power the flow of the slurry through the liquid pump, or to install the storage tank, the first level to n-level heat-retaining reaction tank, and the first level to n-level heat-retaining reaction tank from high to low, and use gravity to power the movement of the slurry, and install a control valve to control the flow of the slurry.

[0026] In actual production, secondary aluminum ash is generally treated in a continuous manner, that is, secondary aluminum ash and water are supplied through the supply port while the material is discharged from the n-class heat-insulating reaction tank so as to ensure continuous production.

[0027] In some embodiments of the present disclosure, the time from providing the secondary aluminum ash to the storage tank to blending the raw materials to form the fifth slurry is 30 minutes to 600 minutes.

[0028] By limiting the time from material supply to material discharge, the time that the slurry remains in each tank body, including the temperature-raising reaction tank and the temperature-retaining reaction tank, can be limited, and the slurry can be positioned at a controlled reaction stage in each tank body.

[0029] In actual production, the time can also be adjusted by the temperature and the amounts of stabilizer and activator added.

[0030] In some embodiments of the present disclosure, in step S2, the mass ratio of secondary aluminum ash to water is set to 1:(1 to 5).

[0031] The purpose of controlling the ratio of secondary aluminum ash to water is to adjust the properties of the first slurry, such as its concentration and viscosity, so that the first slurry can be easily input into the next device.

[0032] In some embodiments of the present disclosure, the volume of each slurry in the storage tank, each temperature-elevating reaction tank, and each temperature-maintaining reaction tank is 30% to 50%.

[0033] The purpose of setting the volume of each slurry to 30% to 50% of the volume of the storage tank, each temperature-raising reaction tank and each heat-retaining reaction tank is to control the volumetric ratio of the slurry in each tank, thereby preventing a large amount of gas generated by stirring during the reaction of the slurry from rising the liquid level in the tank and affecting the discharge of gas, and / or preventing the slurry from clogging the first exhaust port and / or the second exhaust port.

[0034] In some embodiments of the present disclosure, X=A+B, where A is the mass ratio of elemental Al to the secondary aluminum ash, B is the mass ratio of Al4C3 to the secondary aluminum ash, and X≦10%.

[0035] The purpose of controlling X≦10% is to control the mass content of elemental Al and Al4C3 in the secondary aluminum ash, thereby reducing the amount of heat released during hydrolysis and avoiding the impact on AlN hydrolysis during the temperature-raising reaction stage. In some embodiments, the content of elemental Al and Al4C3 in the secondary aluminum ash separated by the ball mill sieve is 10% or less. In some embodiments of the present disclosure, the temperature in the storage tank is controlled to 10°C to 30°C.

[0036] The purpose of controlling the temperature of the storage tank is to slow down the reaction rate of the secondary aluminum ash in the storage tank and to minimize the reaction of the secondary aluminum ash in the storage tank.

[0037] To control the temperature of the storage tank, a cooling device may be installed. For example, the temperature may be reduced by a circulating water cooling system.

[0038] In some embodiments of the present disclosure, the temperatures of the temperature-regulating reaction tanks connected in series to each other gradually increase from the first temperature-regulating reaction tank to the nth temperature-regulating reaction tank, and the temperature of the first temperature-regulating reaction tank may be 10°C to 30°C, the temperature of the nth temperature-regulating reaction tank may be 40°C to 60°C, and / or the temperatures of all the heat-retaining reaction tanks may be 90°C to 100°C.

[0039] The temperature of the series-connected temperature-programmed reaction tanks gradually increases from the first to the nth temperature-programmed reaction tanks, which helps to promote the sequential hydrolysis of elemental Al and Al4C3. If the temperature of the temperature-programmed reaction tank is too low, it will not be effective in promoting the hydrolysis of elemental Al and Al4C3, and if it is too high, it may lead to the hydrolysis of a large amount of AlN.

[0040] In the heated reaction tank, a relatively high temperature helps AlN to be fully hydrolyzed.

[0041] In some embodiments of the present disclosure, the stabilizer includes at least one of calcium dihydrogen phosphate, calcium hydroxyphosphate, ferric ammonium citrate, and sodium alginate; and / or the activator includes at least one of steel slag powder, dry desulfurized ash, modified bentonite, and hydroxyapatite; and / or the demineralizing agent includes at least one of polyaluminum silicate iron sulfate, fly ash, and desulfurized gypsum.

[0042] In some embodiments of the present disclosure, the amount of stabilizer added is 0.5% to 1.5% of the mass of the secondary aluminum ash, and / or the amount of activator added is 0.5% to 2% of the mass of the secondary aluminum ash, and / or the amount of demineralizer added is 0.5% to 1.5% of the mass of the secondary aluminum ash.

[0043] The main role of the stabilizer is to disperse the aluminum ash and fine particles, ensuring sufficient dispersion of the slurry, and to suppress the hydrolysis reaction of AlN, thereby enabling the selective hydrolysis of elemental Al and Al4C3 and the stable release of a flammable gas mixture of H2 and CH4. However, adding a small amount of stabilizer can easily lead to a large amount of AlN hydrolyzing and reacting in the secondary aluminum ash, and adding a relatively large amount can make it difficult for the AlN to react when the temperature rises.

[0044] The main role of the activator is to prevent the formation of a gel coating film from aluminum hydroxide produced by the hydrolysis of AlN, to break down the aluminum hydroxide gel coating film, and to promote sufficient contact between AlN and water. However, if the amount of activator is too high, the primary reaction becomes too violent, making it difficult to adjust and control the reaction temperature, and too many impurity components are incorporated, while if the amount of activator is too low, the efficiency of the AlN hydrolysis reaction is affected.

[0045] The main role of the dechlorinating agent is to increase the particle size of the high-aluminum material after reaction with the secondary aluminum ash, improve the filtration performance of the slurry, reduce the generation of fine particles, promote the precipitation of soluble salts from the aluminum ash particles, increase the dechlorination efficiency, and reduce the water content of the filter cake. However, if the amount of dechlorinating agent is too high, the resulting high-aluminum material will contain too many impurities. If the amount of dechlorinating agent is too low, the filtration performance of the slurry will decrease, the filtered filter cake will have a high water content, and the salt content of the high-aluminum material will increase, which will be detrimental to the drying and use of the high-aluminum material.

[0046] Based on the above, the present disclosure will be further described with reference to specific examples. It should be understood that these examples are only for the purpose of illustrating the present disclosure and are not intended to limit the scope of the present disclosure. Tests under specific conditions not specified in the following examples can generally be performed in accordance with national standards. If there is no corresponding national standard, they can be performed in accordance with common international standards, normal conditions, or conditions recommended by the manufacturer.

[0047] Example 1 The present disclosure provides an apparatus and method for treating secondary aluminum ash, which includes a secondary aluminum ash having a mass content of AlN of 13.72% and a total mass content of elemental Al and Al4C3 of 1.25%. 2 The result calculated using this formula and rounded off to the nearest integer is 1. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in secondary aluminum ash.

[0048] The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer, and Z is the mass ratio of AlN to the secondary aluminum ash.

[0049] That is, the secondary aluminum ash treatment device includes a first-class heating reaction tank and first-class to fourth-class heat-retaining reaction tanks.

[0050] The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are weighed out in a 1:1 mass ratio and delivered to a storage tank. The raw materials are then blended to obtain a slurry. The volume of the slurry in the storage tank and each reaction tank is 50% when delivered. The temperature of the slurry is controlled at 30°C when blending with the raw materials in the storage tank. The slurry then enters the first heating reaction tank, where calcium dihydrogen phosphate is delivered. The calcium dihydrogen phosphate is delivered at a rate of 0.5% of the secondary aluminum ash mass. The slurry enters the first heating reaction tank from the storage tank, where its temperature rises to 40°C. It then enters the first through fourth heat-retention reaction tanks, each maintained at a temperature of 90°C. Hydroxyapatite is then delivered to the first heat-retention reaction tank (first heat-retention reaction tank). Fly ash is delivered to the final heat-retention reaction tank (fourth heat-retention reaction tank). The amount of hydroxyapatite added is 0.85% of the mass of the secondary aluminum ash. The amount of fly ash added is 1% of the mass of the secondary aluminum ash. The time from supplying the secondary aluminum ash raw material to the storage tank to forming the fifth slurry is 310 minutes. The gas generated in the first-class heating reaction tank is cooled and collected, then enters the combustible gas collection system and is burned as fuel. The volume ratio of hydrogen in the collected gas is 88.12%, and the volume ratio of methane is 5.28%. The volume ratio of ammonia in the gas generated in the first-class to fourth-class heating reaction tanks is 96.43%. The ammonia is used to produce ammonium hydroxide in a cooling water absorption system. The reacted slurry is separated into solids and liquids to obtain a filter cake. The filter cake has a water content of 21.36%. The filter cake is dried to obtain recycled high-aluminum material. In the recycled high-aluminum material, the mass content of AlN is 0.152%, the total mass content of elemental Al and Al4C3 is 0.052%, and the mass content of soluble salts is 0.291%.

[0051] Example 2 The secondary aluminum ash treatment device and treatment method provided in the embodiments of the present disclosure are as follows.

[0052] Secondary aluminum ash is provided, in which the mass content of AlN is 32.63%, and the total mass content of elemental Al and Al4C3 is 3.48%. 0.45+58×X-260×X 2 The result calculated using this formula and rounded off to the nearest integer is 2. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in secondary aluminum ash.

[0053] The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer, 8, where Z is the mass ratio of AlN to secondary aluminum ash.

[0054] That is, the secondary aluminum ash treatment device includes the first-class heating reaction tank to the second-class heating reaction tank and the first-class heat-retaining reaction tank to the eighth-class heat-retaining reaction tank.

[0055] The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are weighed in a mass ratio of 1:4 and fed into a storage tank, where the raw materials are blended to obtain a slurry. The volume of the slurry in the storage tank and each reaction tank is 40% when it is delivered. The temperature of the slurry blended with the raw materials in the storage tank is controlled at 23°C. The slurry then enters the first and second heating reaction tanks, where ferric ammonium citrate is fed to the first heating reaction tank. The amount of ferric ammonium citrate fed is 0.8% of the mass of the secondary aluminum ash. After reacting in the first and second temperature-raising reaction tanks, the slurry temperature rises from 23°C to 45°C and then enters the first through eighth temperature-retaining reaction tanks, where the temperature is maintained at 95°C. Dry desulfurized ash is supplied to the first temperature-retaining reaction tank (first temperature-retaining reaction tank), and desulfurized gypsum is supplied to the last temperature-retaining reaction tank (eighth temperature-retaining reaction tank). The dry desulfurized ash is added at 2.0% of the mass of the secondary aluminum ash, and the desulfurized gypsum is added at 1.2% of the mass of the secondary aluminum ash. The secondary aluminum ash takes 600 minutes from the time it is supplied as raw material to the storage tank to form the fifth slurry. The gases generated in the first and second temperature-raising reaction tanks are cooled and collected, then enter the combustible gas collection system and burned as fuel. The volume ratio of hydrogen in the collected gas was 85.36%, and the volume ratio of methane was 12.52%. The volume ratio of ammonia in the gas generated in the first to eighth class thermal insulation reaction tanks was 97.15%. The ammonia was separated into ammonium hydroxide using a cooling water absorption system. The reacted slurry was separated into solids and liquids, and the separated filter cake had a water content of 19.78%. The filter cake was dried to obtain recycled high-aluminum material. The recycled high-aluminum material had a mass content of AlN of 0.257%, a total mass content of elemental Al and Al4C3 of 0.103%, and a mass content of soluble salts of 0.225%.

[0056] Example 3 The secondary aluminum ash treatment device and treatment method provided in this embodiment are as follows:

[0057] Secondary aluminum ash is provided, in which the mass content of AlN is 27.63%, and the total mass content of elemental Al and Al4C3 is 5.94%. 0.45+58×X-260×X 2 The result calculated using this formula and rounded off is an integer of 3. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in secondary aluminum ash. The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer of 7, where Z is the mass ratio of AlN to secondary aluminum ash.

[0058] That is, the secondary aluminum ash treatment device includes the first to third class heating reaction tanks and the first to seventh class heat-retaining reaction tanks.

[0059] The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are weighed in a mass ratio of 1:5 and fed into a storage tank to be blended with the raw materials. The slurry occupies 30% of the volume of the storage tank and each reaction tank when it is delivered. The temperature of the slurry is controlled at 15°C when blending with the raw materials in the storage tank. The slurry enters the first to third heating reaction tanks, and calcium hydroxyphosphate is fed to the first heating reaction tank. The calcium hydroxyphosphate is fed in an amount of 1.2% of the mass of the secondary aluminum ash. After reacting in the first to third heating reaction tanks, the slurry's temperature rises from 15°C to 55°C and then enters the first to seventh heating reaction tanks, where it is maintained at a temperature of 92°C. Modified bentonite is supplied to the first thermally-insulated reaction tank (Class 1 thermally-insulated reaction tank), and fly ash is supplied to the last thermally-insulated reaction tank (Class 7 thermally-insulated reaction tank). The amount of modified bentonite added is 1.5% of the mass of secondary aluminum ash, and the amount of fly ash added is 0.7% of the mass of secondary aluminum ash. The time from supplying the secondary aluminum ash raw material to the storage tank to forming the fifth slurry is 450 minutes. The gases generated in the Class 1 to Class 3 thermally-insulated reaction tanks are collected after cooling and then enter the combustible gas collection system to be burned as fuel. The collected gases are 90.31% hydrogen by volume and 4.56% methane by volume. The gases generated in the Class 1 to Class 7 thermally-insulated reaction tanks are 95.34% ammonia by volume. The ammonia is absorbed by dilute sulfuric acid to produce ammonium sulfate. The reacted slurry is subjected to solid-liquid separation, and the separated filter cake has a water content of 24.59%. The filter cake is dried to obtain a recycled high-aluminum material. In the recycled high-aluminum material, the mass content of AlN is 0.213%, the total mass content of elemental Al and Al4C3 is 0.097%, and the mass content of soluble salts is 0.281%.

[0060] Example 4 The secondary aluminum ash treatment device and treatment method provided in this embodiment are as follows:

[0061] Provide secondary aluminum ash, which has a mass content of AlN of 22.76% and a total mass content of elemental Al and Al4C3 of 9.56%. 0.45+58×X-260×X 2 The result calculated using this formula and rounded off is an integer of 4. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in secondary aluminum ash. The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer, and Z is the mass ratio of AlN to secondary aluminum ash.

[0062] That is, the secondary aluminum ash treatment device includes the first to fourth class heating reaction tanks and the first to sixth class heat-retaining reaction tanks.

[0063] The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are fed into the storage tank in a mass ratio of 1:3 to blend the raw materials. The slurry occupies 35% of the volume in the storage tank and each reaction tank when it is fed. The temperature of the slurry is controlled at 18°C ​​when blending the raw materials in the storage tank. The slurry enters the first to fourth heating reaction tanks, and sodium alginate is fed to the first heating reaction tank, with the sodium alginate being fed in an amount of 1.5% of the mass of the secondary aluminum ash. After reacting in the first to fourth heating reaction tanks, the slurry's temperature rises from 18°C ​​to 50°C and then enters the first to sixth heating reaction tanks, where it is maintained at a temperature of 98°C. Steel slag powder is supplied to the first heat-insulating reaction tank (Class 1 heat-insulating reaction tank), and polyaluminum silicate ferrous sulfate is supplied to the last heat-insulating reaction tank (Class 6 heat-insulating reaction tank). The amount of steel slag powder added is 1.35% of the mass of secondary aluminum ash, and the amount of polyaluminum silicate ferrous sulfate added is 0.5% of the mass of secondary aluminum ash. The time from supplying the secondary aluminum ash to the storage tank to forming the fifth slurry is 480 minutes. The gases generated in the Class 1 to Class 4 heat-insulating reaction tanks are cooled and collected, then enter the combustible gas collection system and burned as fuel. The collected gases are 84.72% hydrogen by volume and 10.27% methane by volume. The gases generated in the Class 1 to Class 6 heat-insulating reaction tanks are 98.67% ammonia by volume. The ammonia is absorbed by dilute sulfuric acid to produce ammonium sulfate. The reacted slurry was subjected to solid-liquid separation, and the separated filter cake had a water content of 20.41%. The filter cake was then dried to obtain a recycled high-aluminum material. In the recycled high-aluminum material, the mass content of AlN was 0.182%, the total mass content of elemental Al and Al4C3 was 0.127%, and the mass content of soluble salts was 0.245%.

[0064] Example 5 The secondary aluminum ash treatment device and treatment method provided in this embodiment are as follows: Provide secondary aluminum ash, which has a mass content of AlN of 6.35% and a total mass content of elemental Al and Al4C3 of 7.32%. 0.45+58×X-260×X 2 The result calculated using this formula and rounded off is an integer of 3. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in secondary aluminum ash. The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer, and Z is the mass ratio of AlN to the secondary aluminum ash.

[0065] That is, the secondary aluminum ash treatment device includes the first to third temperature-raising reaction tanks and the first to third temperature-retaining reaction tanks.

[0066] The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are weighed in a mass ratio of 1:2 and fed into a storage tank to blend the raw materials. The slurry occupies 45% of the volume in the storage tank and each reaction tank when it is delivered. The temperature of the slurry is controlled at 10°C when blending the raw materials in the storage tank. The slurry enters the first to third heating reaction tanks, and calcium hydroxyphosphate is fed to the first heating reaction tank. The calcium hydroxyphosphate is fed in an amount of 1.3% of the mass of the secondary aluminum ash. After reacting in the first to third heating reaction tanks, the slurry is heated from 10°C to 60°C and then enters the first to third heat-retaining reaction tanks, where it is maintained at a temperature of 100°C. Hydroxyapatite is supplied to the first thermally-insulated reaction tank (Class 1 thermally-insulated reaction tank), and fly ash is supplied to the last thermally-insulated reaction tank (Class 3 thermally-insulated reaction tank). The amount of hydroxyapatite added is 0.5% of the mass of the secondary aluminum ash, and the amount of fly ash added is 1.5% of the mass of the secondary aluminum ash. The time from supplying the secondary aluminum ash raw material to the storage tank to forming the fifth slurry is 360 minutes. The gases generated in the Class 1 to Class 3 thermally-insulated reaction tanks are cooled and collected, then enter the combustible gas collection system and burned as fuel. The volume ratio of the collected gases is 85.39% hydrogen and 9.63% methane. The volume ratio of ammonia in the gases generated in the Class 1 to Class 6 thermally-insulated reaction tanks is 96.25% ammonia. Ammonia is then used to produce ammonium hydroxide through a cooling absorption system. The reacted slurry is subjected to solid-liquid separation, and the separated filter cake has a water content of 18.67%. The filter cake is dried to obtain a recycled high-aluminum material. In the recycled high-aluminum material, the mass content of AlN is 0.227%, the total mass content of elemental Al and Al4C3 is 0.143%, and the mass content of soluble salts is 0.177%.

[0067] Comparison 1 The secondary aluminum ash treatment device and treatment method provided in this comparative example are as follows: Secondary aluminum ash is provided, in which the mass content of AlN is 32.63%, and the total mass content of elemental Al and Al4C3 is 3.48%. 0.45+58×X-260×X 2 The result calculated using this formula and rounded off to the nearest integer is 2. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in the secondary aluminum ash.

[0068] The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer, 8, where Z is the mass ratio of AlN to secondary aluminum ash.

[0069] That is, the secondary aluminum ash treatment device includes two heating reaction tanks and eight heat-retaining reaction tanks. The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are weighed in a mass ratio of 1:4 and fed into a storage tank to blend the raw materials. The slurry occupies 40% of the volume in the storage tank and each reaction tank when it is delivered. The temperature of the slurry is controlled at 23°C when blending the raw materials in the storage tank. The slurry enters the first and second temperature-raising reaction tanks, and ferric ammonium citrate is fed to the first temperature-raising reaction tank at a rate of 0.8% of the mass of the secondary aluminum ash. After reacting in the first and second temperature-raising reaction tanks, the slurry's temperature rises from 23°C to 45°C and then enters the first to eighth temperature-retaining reaction tanks, where it is maintained at a temperature of 95°C. Desulfurized gypsum is supplied only to the last heat-insulating reaction tank (Class 8 heat-insulating reaction tank), and the amount of desulfurized gypsum added is 1.2% of the mass of secondary aluminum ash. The time from supplying the secondary aluminum ash to the storage tank to forming the fifth slurry is 310 minutes. The gases generated in the Class 1 and Class 2 heat-insulating reaction tanks are cooled and collected, then fed into the combustible gas collection system for combustion as fuel. The collected gases are 85.79% hydrogen by volume and 11.25% methane by volume. The gases generated in the Class 1 to Class 8 heat-insulating reaction tanks are 95.63% ammonia by volume. The ammonia is used to produce ammonium hydroxide via a cooling water absorption system. The reacted slurry undergoes solid-liquid separation, and the separated filter cake has a water content of 23.32%. The filter cake is dried to obtain recycled high-aluminum material. In the recycled high-aluminum material, the mass content of AlN is 3.56%, the total mass content of elemental Al and Al4C3 is 0.128%, and the mass content of soluble salts is 0.257%.

[0070] Comparison 2 The secondary aluminum ash treatment device and treatment method provided in this comparative example are as follows:

[0071] Secondary aluminum ash is provided, in which the mass content of AlN is 27.63%, and the total mass content of elemental Al and Al4C3 is 5.94%. 0.45+58×X-260×X 2 The result calculated using this formula and rounded off is an integer of 3. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in secondary aluminum ash.

[0072] The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer, 7, where Z is the mass ratio of AlN to secondary aluminum ash.

[0073] That is, the secondary aluminum ash treatment device includes the first to third class heating reaction tanks and the first to seventh class heat-retaining reaction tanks. The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are weighed in a mass ratio of 1:5 and fed into a storage tank to be blended with the raw materials. The slurry occupies 30% of the volume in the storage tank and each reaction tank when it is delivered. The temperature of the slurry is controlled at 15°C when blending with the raw materials in the storage tank. The slurry enters the first to third heating reaction tanks, and calcium hydroxyphosphate is fed to the first heating reaction tank. The calcium hydroxyphosphate is fed in an amount of 1.2% of the mass of the secondary aluminum ash. After reacting in the first to third heating reaction tanks, the temperature of the slurry rises from 15°C to 55°C. It then enters the first to seventh heating reaction tanks, where it is maintained at a temperature of 92°C. Modified bentonite was supplied only to the first heat-insulating reaction tank (Class 1 heat-insulating reaction tank), with the amount of modified bentonite added being 1.5% of the mass of secondary aluminum ash. The time from supplying the secondary aluminum ash to the storage tank to forming the fifth slurry was 600 minutes. The gases generated in the Class 1 to Class 3 heat-insulating reaction tanks were cooled and collected, then fed into the combustible gas collection system for combustion as fuel. The volume ratio of the collected gases was 89.65% hydrogen and 3.72% methane. The volume ratio of ammonia in the gases generated in the Class 1 to Class 7 heat-insulating reaction tanks was 97.43%. The ammonia was absorbed by dilute sulfuric acid to produce ammonium sulfate. The reacted slurry was subjected to solid-liquid separation, and the separated filter cake had a water content of 31.24%. The filter cake was dried to obtain recycled high-aluminum material. In the recycled high-aluminum material, the mass content of AlN is 0.231%, the total mass content of elemental Al and Al4C3 is 0.147%, and the mass content of soluble salts is 0.744%.

[0074] Comparison 3 The secondary aluminum ash treatment device and treatment method provided in this comparative example are as follows:

[0075] Provide secondary aluminum ash, which has a mass content of AlN of 22.76% and a total mass content of elemental Al and Al4C3 of 9.56%. 0.45+58×X-260×X 2 The result calculated using this formula and rounded off is an integer of 4. Of these, X = A + B, where A is the mass ratio of elemental Al to secondary aluminum ash, and B is the mass ratio of Al4C3 to secondary aluminum ash, i.e., X is the total mass content of elemental Al and Al4C3 in secondary aluminum ash.

[0076] The result calculated using the formula 22 × Z + 1.2 is rounded to the nearest integer, and Z is the mass ratio of AlN to secondary aluminum ash.

[0077] That is, the secondary aluminum ash treatment device includes the first to fourth class heating reaction tanks and the first to sixth class heat-retaining reaction tanks.

[0078] The secondary aluminum ash is treated using the following method. Secondary aluminum ash and water are weighed in a mass ratio of 1:3 and fed into a storage tank for blending. The slurry occupies 35% of the storage tank and each reaction tank's volume when delivered. The temperature of the slurry is controlled at 18°C ​​when blending with the raw materials in the storage tank. The slurry then enters the first through fourth heating reaction tanks. After reacting in the first through fourth heating reaction tanks, the temperature of the slurry rises from 18°C ​​to 50°C. It then enters the first through sixth heat-retaining reaction tanks, where it is maintained at 98°C. Steel slag powder is supplied to the first heat-insulating reaction tank (Class 1 heat-insulating reaction tank), and polyaluminum silicate ferrous sulfate is supplied to the last heat-insulating reaction tank (Class 6 heat-insulating reaction tank). The amount of steel slag powder added is 1.35% of the mass of secondary aluminum ash, and the amount of polyaluminum silicate ferrous sulfate added is 0.5% of the mass of secondary aluminum ash. The time from supplying the secondary aluminum ash raw material to the storage tank to forming the fifth slurry is 450 minutes. The gases generated in the Class 1 to Class 4 heat-insulating reaction tanks are cooled and collected, then enter the combustible gas collection system and burned as fuel. The volume ratio of the collected gases is 72.34% hydrogen and 3.12% methane. The volume ratio of ammonia in the gases generated in the Class 1 to Class 6 heat-insulating reaction tanks is 88.15% ammonia. The ammonia is absorbed by dilute sulfuric acid to produce ammonium sulfate. The reacted slurry is subjected to solid-liquid separation, and the separated filter cake has a water content of 23.98%. The filter cake is dried to obtain a recycled high-aluminum material. In the recycled high-aluminum material, the mass content of AlN is 0.296%, the total mass content of elemental Al and Al4C3 is 1.781%, and the mass content of soluble salts is 0.233%.

[0079] Related study effects and data As can be seen from the above examples and comparative examples, when the secondary aluminum ash treatment device and treatment method provided in the examples of the present disclosure were used, the reacted slurry was subjected to solid-liquid separation, and the resulting filter cake had a water content of <25%, an AlN mass content of <0.3%, a total mass content of elemental Al and Al4C3 of <0.2%, a soluble salt mass content of <0.1%, a hydrogen to methane volume ratio of >93% in the gas collected from the heating reaction tank, and an ammonia volume ratio of >95% in the gas collected from the heating reaction tank. Comparative Examples 1, 2, and 3 were based on Examples 2, 3, and 4, but did not include the addition of an activator, demineralizer, or stabilizer. The treatment effects were significantly different. In Comparative Example 1, no activator was added, and the AlN mass content of the recycled high-aluminum material obtained by drying the filter cake was 3.56%, far greater than the effect of adding an activator. In Comparative Example 2, no desalting agent was added, so the reacted slurry was separated into solids and liquids, resulting in a filter cake with a water content of 31.24%. The recycled high-aluminum material obtained by drying the filter cake had a soluble salt mass content of 0.744%. The filter cake showed relatively poor dehydration and desalting effects. In Comparative Example 3, no stabilizer was added, so the recycled high-aluminum material had a total mass content of elemental Al and Al4C3 of 1.781%, resulting in relatively poor hydrolysis of elemental Al and Al4C3.

[0080] Each embodiment in the present disclosure may be expressed in the form of a range. It should be understood that, for convenience and brevity, a range is described, but this should not be construed as a necessary limitation on the scope of the present disclosure. Thus, the description of a range should be understood as having specifically disclosed all possible subranges and single numerical values ​​within that range. For example, a description of a range of 1 to 6 should be understood as having specifically disclosed subranges such as 1 to 3, 1 to 4, 1 to 5, 2 to 4, 2 to 6, 3 to 6, etc., as well as single numerical values ​​within that range, such as 1, 2, 3, 4, 5, and 6. Any and all ranges may be applied. Furthermore, whenever a range of values ​​is recited herein, it is meant to include any recited numerical values ​​(fractional or integer) within that range.

[0081] In this disclosure, unless otherwise specified, directional expressions such as "top" and "bottom" refer to the directions specifically shown in the drawings. Furthermore, in the description of the specification of this disclosure, terms such as "including" and "include" mean "including, but not limited to, XXX." Furthermore, terms such as "including" and "comprises" or any similar term are intended to encompass a non-exclusive inclusion, and a process, method, article, or device that includes a set of elements may further include, in addition to those elements, other elements not expressly listed, or elements inherent to the process, method, article, or device. Unless further limited, an element defined by a sentence "comprising XXX" does not exclude the process, method, article, or device that includes the element from further including other identical elements. In this specification, terms indicating relationships, such as "first" and "second," are used solely to distinguish one entity or operation from another, and do not require or imply any actual relationship or order between these entities or operations. As used herein, the term "and / or" expressing a relationship between related objects indicates that three relationships may exist. For example, A and / or B means that only A may exist, both A and B may exist simultaneously, or only B may exist. A relationship between three or more related objects described with "and / or" indicates that only one of the three related objects may exist, or at least two of the three related objects may exist simultaneously. For example, A and / or B and / or C means that only one of A, B, and C may exist, or any two of them may exist simultaneously, or all three of them may exist simultaneously. As used herein, "at least one" means one or more, and "multiple" means two or more. The terms "at least one," "hereinafter, at least one (one item)," and other similar expressions refer to any combination of these items, including any combination of one item or multiple items.For example, "at least one of a, b, or c" or "at least one of a, b, and c" each represents a, b, c, ab (i.e., a and b), ac, bc, or abc, where a, b, and c may each be one or more.

[0082] The foregoing description is merely of specific embodiments of the present disclosure, intended to enable those skilled in the art to understand or practice the present disclosure. Many variations on these embodiments will be apparent to those skilled in the art. The general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present disclosure. Therefore, the present disclosure is not limited to the embodiments disclosed herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. a storage tank, a temperature-raising reaction means, and a temperature-retaining reaction means, which are sequentially connected to each other; The storage tank is provided with a supply port for supplying aluminum ash, The temperature-raising reaction means includes n temperature-raising reaction tanks connected in series, each of which is a first-class temperature-raising reaction tank, a second-class temperature-raising reaction tank, ... an n-th class temperature-raising reaction tank, and each of the n temperature-raising reaction tanks connected in series is provided with a first exhaust port for discharging gas, The heat-retaining reaction means includes m heat-retaining reaction tanks connected in series, each of which is a first-class heat-retaining reaction tank, a second-class heat-retaining reaction tank, ... an m-th class heat-retaining reaction tank, and each of the m heat-retaining reaction tanks connected in series is provided with a second exhaust port for discharging gas. supplying secondary aluminum ash and water through the supply port into the storage tank to form a first slurry in the storage tank; While guiding the first slurry into the first temperature-raising reaction tank, simple Al and Al are introduced into the first temperature-raising reaction tank. ４ C ３ providing a stabilizer to promote hydrolysis of AlN while inhibiting hydrolysis of AlN to form a second slurry; allowing the second slurry to flow from the first temperature-rising reaction tank to the nth temperature-rising reaction tank, forming a third slurry in the nth temperature-rising reaction tank, and collecting gas generated by the reaction from the first temperature-rising reaction tank into the nth temperature-rising reaction tank; supplying an activator for increasing the hydrolysis activity of AlN to the first heat-retaining reaction tank while guiding the third slurry to the first heat-retaining reaction tank to form a fourth slurry; The fourth slurry is allowed to flow from the first-class heat-retaining reaction tank to the n-class heat-retaining reaction tank, and a dechlorinating agent is supplied to the n-class heat-retaining reaction tank to promote the precipitation of salt substances while increasing the particle size of solid particles, and the dechlorinating agent and the fourth slurry are mixed and reacted to form a fifth slurry, and the gas generated by the reaction in the first-class heat-retaining reaction tank to the n-class heat-retaining reaction tank is collected; filtering the fifth slurry to obtain a filtrate, and concentrating the filtrate to perform crystallization.

2. The n is 0.45 + 58 × X - 260 × X ２ The result is calculated using the formula and rounded to the nearest integer. X = A + B, where A is the mass ratio of elemental aluminum to secondary aluminum ash, and B is the mass ratio of Al in secondary aluminum ash. ４ C ３ 2. The method for treating secondary aluminum ash according to claim 1, wherein the mass ratio of the secondary aluminum ash is 1 / 2 or more.

3. The m is an integer obtained by rounding off the result of calculation using the formula 22 × Z + 1.2, 2. The method for treating secondary aluminum ash according to claim 1, wherein Z is the mass ratio of AlN to the secondary aluminum ash.

4. 2. The method for treating secondary aluminum ash according to claim 1, wherein the time from supplying the material to the storage tank to forming the fifth slurry is 30 to 600 minutes.

5. X = A + B, A is the mass ratio of elemental aluminum to secondary aluminum ash, and B is the mass ratio of Al in secondary aluminum ash. ４ C ３ 5. The method for treating secondary aluminum ash according to claim 4, wherein X is the mass ratio of the secondary aluminum ash to the total mass of the secondary aluminum ash, and X≦10%.

6. 5. The method for treating secondary aluminum ash according to claim 4, wherein the temperature in the storage tank is controlled to be between 10°C and 30°C.

7. The temperature from the first temperature-rising reaction tank to the nth temperature-rising reaction tank is gradually increased, and the temperature of the first temperature-rising reaction tank is 10°C to 30°C, and the temperature of the nth temperature-rising reaction tank is 40°C to 60°C; and / or The method for treating secondary aluminum ash according to claim 4, characterized in that the temperature of all of the heat-retaining reaction tanks is 90°C to 100°C.

8. the stabilizing agent comprises at least one of calcium dihydrogen phosphate, calcium hydroxyphosphate, ferric ammonium citrate, sodium alginate; and / or The activator includes at least one of iron and steel slag powder, dry desulfurized ash, modified bentonite, and hydroxyapatite; and / or 5. The method for treating secondary aluminum ash according to claim 4, wherein the dechlorinating agent includes at least one of polysilicate aluminum iron sulfate, fly ash, and desulfurized gypsum.

9. The amount of the stabilizer added is 0.5% to 1.5% of the mass of the secondary aluminum ash, and / or The amount of the activator added is 0.5% to 2% of the mass of the secondary aluminum ash, and / or 9. The method for treating secondary aluminum ash according to claim 8, wherein the amount of the stabilizer added to the dechlorinating agent is 0.5% to 1.5% of the mass of the secondary aluminum ash.

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