Resource utilization method for co-removal of dioxins by carrier flotation of waste incineration fly ash

Abstract

This invention discloses a resource utilization method for co-removing dioxins from waste incineration fly ash using carrier flotation, comprising the following steps: 1) adding waste incineration fly ash to water, thoroughly stirring and dispersing it, and then performing magnetic separation to obtain magnetic tailings slurry; 2) filtering the magnetic tailings slurry to obtain desalination filter cake; 3) mixing the desalination filter cake with anthracite slime concentrate and then co-grinding it; 4) performing flotation on the ground slurry to obtain concentrate product K2 and flotation tailings. This invention couples carrier flotation of anthracite slime concentrate with strong magnetic separation pre-desalination, solving industry pain points such as the difficulty in flotation of ultrafine activated carbon, the inability to remove dioxins at their source, and high salt interference in separation. It constructs a closed-loop process of "magnetic separation-salt separation-grinding-carrier flotation-heavy metal removal," achieving resource utilization of all components of fly ash at low temperatures, and allowing tailings to be directly discharged in compliance with standards. The process is mature, easy to implement, requires low investment, has low cost, and can be scaled up, resulting in significant economic and environmental benefits.

Description

Technical Field

[0001] This invention belongs to the technical field of hazardous waste harmless disposal and resource utilization, specifically involving a resource utilization method for the synergistic removal of dioxins by carrier flotation of fly ash from waste incineration; in particular, it involves an integrated full-process technology combining strong magnetic separation followed by salt separation, synergistic grinding activation, anthracite slime carrier flotation, and deep flotation of heavy metals, which can simultaneously achieve the recovery of magnetic valuable components from fly ash, separation of soluble salts, efficient and deep removal of dioxins by ultrafine activated carbon, deep purification of heavy metals, and compliant discharge of tailings. Background Technology

[0002] The statements in this section are merely background information related to the present invention and do not necessarily constitute prior art.

[0003] Waste-to-energy incineration has become the mainstream approach for the disposal of municipal solid waste in megacities due to its advantages of significant volume reduction, thorough harmlessness, and recyclable energy. The flue gas generated by the incineration system is purified through a semi-dry desulfurization tower → activated carbon injection device → bag filter. The fine particulate matter, desulfurization reaction products, incompletely reacted alkaline agents, saturated powdered activated carbon, heavy metal-rich particles, and a small amount of unburned carbon components collected by the bag filter collectively form incineration fly ash. Fly ash accounts for approximately 10%–20% of the total incineration ash and belongs to HW18 category hazardous waste in the National Hazardous Waste List. Its complex composition, high pollutant concentration, and significant environmental risks make it a core bottleneck restricting the sustainable development of the industry.

[0004] Fly ash contains 20%–40% CaO, 10%–25% SiO2, and 35%–15% Al2O3, with the inorganic framework accounting for 60%–80% of the total. The high CaO content primarily stems from the large-scale injection of alkaline absorbents in the desulfurization system, resulting in a pH of 11–13 in the fly ash leachate, exhibiting strong alkalinity. Fly ash also has extremely high soluble salt content (generally 10%–30% of the total mass, sometimes reaching 45%–55%), existing in the form of NaCl, KCl, and CaCl2. The chloride ion content can reach 10%–20%, originating from the high-temperature decomposition and condensation enrichment of components such as kitchen waste and chlorinated plastics. High salt content and high alkalinity not only easily lead to salt-out cracking of the solidified body and exacerbate the risk of heavy metal leaching, but also severely affect the hydrophobicity and floatability of particles during flotation. If flotation is used, these are components that must be preferentially removed or reduced.

[0005] Regarding heavy metal pollution, the levels of Pb, Cd, Zn, Cu, Cr, and Hg in fly ash are 10 to 100 times higher than in normal soil, and their leaching toxicity far exceeds landfill standards, posing a long-term and irreversible threat to the ecosystem. Another more prominent issue is dioxin (PCDD / Fs) concentration in fly ash, typically ranging from 0.1 to 50 ng TEQ / g, far exceeding safe utilization limits. Studies have shown that 70% to 95% of dioxins ultimately accumulate in the activated carbon component of fly ash; therefore, separating activated carbon is crucial for addressing dioxin pollution from fly ash.

[0006] Activated carbon in fly ash is artificially injected in a measured amount into the flue gas purification system. Its purpose is to efficiently adsorb gaseous organic pollutants such as dioxins in the flue gas. After injection, the activated carbon forms a filter cake layer on the surface of the filter bags. When the flue gas passes through, the dioxins are physically and chemically adsorbed and fixed, thus achieving compliant emissions. However, activated carbon has extremely fine particle size (<100μm) and a large specific surface area (500–1500m²). 2 Fly ash, with its high surface energy and strong hydrophobicity, coupled with its particle size mainly concentrated between 4μm and 100μm, and an average particle size of less than 40μm, exhibits irregular particle size, well-developed pores, and a large specific surface area. These fine particle characteristics make conventional sorting methods ineffective in recovering attached carbon and dioxins. For example, when using conventional flotation, these surface properties of fly ash and activated carbon lead to poor reagent selectivity, resulting in extremely limited dioxin removal and a significant increase in reagent dosage. Currently, under low-temperature conditions, conventional flotation can only meet the landfill standard stipulated in the previously abolished national standard GB 16889-2008, which is below 3μg TEQ / kg. However, the currently pilot standard HJ 1134-2020 stipulates that the total amount of dioxin residues in the treated product should not exceed 50 ng-TEQ / kg (based on the dry weight of fly ash), i.e., 0.05μg TEQ / kg, thus imposing new requirements on the dioxin content in the treated product.

[0007] Therefore, with increasingly stringent policies and limited landfill routes, the industry urgently needs an integrated, low-cost treatment system that can simultaneously achieve soluble salt removal, stable recovery of heavy metals, complete separation and degradation of dioxins, and resource utilization of activated carbon. Summary of the Invention

[0008] This invention aims to at least partially solve one of the technical problems in related technologies. Therefore, the main objective of this invention is to provide a resource utilization method for the synergistic removal of dioxins by flotation of waste incineration fly ash carriers, aiming to solve problems in existing waste incineration fly ash treatment technologies, such as the inability to target and separate dioxins from ultrafine activated carbon, high salt interference in flotation, difficulty in deep removal of heavy metals, inability to directly discharge tailings, and high treatment costs.

[0009] The objective of this invention is achieved through the following technical solution: A method for the resource utilization of waste incineration fly ash carrier flotation for synergistic removal of dioxins includes the following steps: 1) High-intensity magnetic separation and desalination: The fly ash from waste incineration is added to water at a solid-liquid mass ratio of 1:5-10, preferably 1:5-8. After thorough stirring and dispersion, the mixture is sent to a high-intensity magnetic separator for magnetic separation to obtain magnetic material product K1 and magnetic separation tailings slurry. The magnetic separation tailings slurry is filtered, and the filtrate is treated with mature technology to recover soluble industrial salts such as NaCl and KCl. The fresh water obtained after separating the soluble industrial salts from the filtrate can be recycled, for example, for pulping, grinding makeup water, flotation, etc. The magnetic product K1 is directly recycled as a valuable component.

[0010] 2) Co-grinding activation: Mix magnetic separation tailings with anthracite slime concentrate, with the amount of slime concentrate added being 2%~10% of the fly ash mass, preferably 2%~5%; add water at a liquid-solid mass ratio of 5~10:1, and carry out co-grinding. Control the grinding fineness so that the mass ratio of materials ≤200 mesh is >85%, so that the particle surface is fully activated and the carrier is evenly dispersed. At the same time, it destroys the pore structure and agglomeration of fly ash, providing a basis for subsequent carrier flotation.

[0011] 3) Carrier flotation for decarbonization and dioxin removal: The slurry after grinding is fed into a flotation machine, and a composite collector is added for flotation; the concentrate product K2 is obtained by flotation, and K2 is returned to the incinerator for high-temperature reburning to achieve complete decomposition of dioxins; the dioxin content of the flotation tailings is sampled and tested.

[0012] The flotation tailings can be further subjected to deep flotation to remove heavy metals. Specifically, the flotation tailings are subjected to existing mature heavy metal flotation processes to remove heavy metals such as Pb, Cd, Zn, Cu, and Cr. At least the heavy metals with leaching activity can be removed, and finally purified tailings with no risk of heavy metal pollution and no dioxin residue can be obtained, which can be directly discharged or used as building material raw materials.

[0013] In some specific embodiments, the anthracite slime concentrate described in step 2) has an ash content of 10-20%, is a gravity separation product, and does not contain any flotation reagents.

[0014] In some specific embodiments, the composite collector in step 3) is at least one of diesel oil, kerosene, and white oil, and a mixture of at least one of No. 2 oil, 2-octanol, and MIBC.

[0015] In some specific implementations, the flotation process in step 3) is a single flotation, with a flotation time of 3 to 5 minutes and a reagent dosage of 1 to 2 kg / t.

[0016] Compared with the prior art, the present invention has at least the following advantages: The present invention provides a resource utilization method for the co-removal of dioxins from waste incineration fly ash using carrier flotation. First, strong magnetic separation is used to recover valuable magnetic components and pre-desalinate, eliminating the strong inhibitory effect of high salt on flotation. Then, co-grinding and activation with anthracite slime gravity concentrate is performed to strengthen the mechanical bond and interfacial interaction between the carrier and ultrafine activated carbon. Finally, anthracite slime is used as a carrier for flotation to efficiently remove activated carbon and dioxins, and subsequent heavy metal flotation achieves complete purification of tailings ash. This invention pioneers a coupled process of carrier flotation of anthracite slime gravity concentrate and strong magnetic separation pre-desalination, solving industry pain points such as the difficulty in flotation of ultrafine activated carbon, the inability to remove dioxins at their source, and high salt interference in separation. It constructs a closed-loop process of "magnetic separation-salt separation-grinding-carrier flotation-heavy metal removal," achieving full component resource utilization of fly ash at low temperatures. Tailings ash can be directly discharged in compliance with standards. The process is mature, easy to implement, requires low investment, has low cost, and can be scaled up, offering significant economic and environmental benefits. Attached Figure Description

[0017] To more clearly illustrate the specific embodiments of the present invention, the accompanying drawings used in the description of the specific embodiments or the prior art will be briefly introduced below.

[0018] Figure 1 The process flow diagram is provided by the present invention for the resource utilization method of co-removal of dioxins by flotation of waste incineration fly ash carrier. Detailed Implementation

[0019] The present invention will be further described in detail below with reference to the accompanying drawings and embodiments. The following embodiments are merely descriptive and not limiting, and should not be construed as limiting the scope of protection of the present invention.

[0020] When a quantity, concentration, or other value or parameter is described as a range, preferred range, or preferred upper and lower limits, it should be understood that it is equivalent to specifically disclosing any range by combining any pair of upper or preferred values ​​with any lower or preferred values, regardless of whether the range is specifically disclosed. Unless otherwise stated, the numerical range values ​​listed herein include the endpoints of the range and all integers and fractions within that range.

[0021] Unless otherwise stated, all percentages, parts, ratios, etc. in this document are by weight.

[0022] The materials, methods, and embodiments described herein are exemplary and should not be construed as limiting unless otherwise stated.

[0023] In the following examples, the fly ash used in waste incineration was taken from a municipal solid waste incineration plant, with an initial dioxin content of 10.33 μg TEQ / kg and a soluble salt content of 45.19%. The anthracite slime concentrate is a product of spiral chute gravity separation with an ash content of 15.57%. Specifically, in the following embodiment, the specific method for preparing the anthracite slime concentrate is as follows: anthracite slime (ash content 56.77%) is mixed with water at a mass ratio of 1:5 to form a slurry. The opening degree of the light component in the spiral chute is controlled at 10%, and spiral separation is carried out under the condition of a flushing water flow rate of 6L / min. The obtained light component minerals are passed through a 150-mesh sieve, and the product on the sieve is the anthracite slime concentrate with an ash content of 15.57%.

[0024] The composite collector is a mixture of diesel oil, white oil, and MIBC in a ratio of 3:1:1, which has both collecting and foaming effects.

[0025] The test methods used in the following embodiments include: 1) Ash content test; Ash content was determined according to the slow ashing method in GB / T 212-2008 "Industrial Analysis Methods for Coal". 1g of sample was weighed into an ash dish using an analytical balance and placed in a muffle furnace. The furnace temperature was slowly raised to 500℃ over 30 minutes and maintained for 30 minutes. The temperature was then slowly raised to 815±10℃ and ignited until the mass was constant. The ash content was determined by the mass fraction of the residue relative to the original sample mass. 2) Calorific value test of refined coal products According to the national standard GB / T 213-2008 "Method for Determination of Calorific Value of Coal", the calorific value was determined according to the principle of the oxygen bomb calorimetry described above. 3) The dioxin toxicity equivalent (TEQ) was determined in accordance with the national standard HJ 77.3-2018 "Determination of dioxins in solid waste by isotope dilution high-resolution gas chromatography-high-resolution mass spectrometry". The goal is to meet the standard specified in HJ 1134-2020 "Technical Specification for Pollution Control of Fly Ash from Municipal Solid Waste Incineration (Trial)", that is, the dioxin content in the treated fly ash is ≤50 ng TEQ / kg (dry basis). The yield is a percentage calculated as the ratio of the concentrate or tailings mass to the sum of the obtained concentrate and tailings mass, i.e., the mass of soluble salts removed.

[0026] Example 1

[0027] This embodiment provides a method for the resource utilization of waste incineration fly ash by flotation to synergistically remove dioxins, which includes the following steps: 1) High-intensity magnetic separation and desalination: Fly ash from waste incineration is added to water at a solid-liquid mass ratio of 1:8, and after thorough stirring and dispersion, it is fed into a wet permanent magnet high-intensity magnetic separator. Magnetic separation is carried out at a magnetic field strength of 1.2T and a drum rotation speed of 30r / min to obtain magnetic product K1 and magnetic separation tailings slurry. The magnetic separation tailings slurry is filtered to obtain filter cake and filtrate. The filtrate is subjected to salt separation treatment to recover soluble industrial salts such as NaCl and KCl. The filter cake is repeatedly soaked and washed with a small amount of clean water, and the wash water is added to the filtrate. 2) Co-grinding activation: The filter cake is mixed with anthracite slime concentrate, wherein the amount of anthracite slime concentrate added is 3% of the mass of the waste incineration fly ash; water is added at a liquid-to-solid mass ratio of 6:1, and co-grinding is carried out to make the mass proportion of material with a grinding fineness of ≤200 mesh 88.02%, so as to fully activate the particle surface, uniformly disperse the carrier, and destroy the pore structure and agglomeration of the waste incineration fly ash, providing a basis for subsequent carrier flotation; 3) Carrier flotation for decarbonization and dioxin removal: The slurry after grinding is fed into the flotation machine, and a composite collector (a mixed collector prepared by diesel oil: white oil: MIBC = 3:1:1) is added for flotation for 5 minutes at a dosage of 1.89 kg / t. The concentrate product K2 is obtained by flotation. The dioxin content is tested by sampling the flotation tailings.

[0028] This application analyzes the concentrate and tailings obtained from flotation in this embodiment, and the specific results are shown in the table below:

[0029] As shown in the table, the processing method of this application can obtain a concentrate product K2 with a certain calorific value, and tailings with a dioxin content of less than 50 ng TEQ / kg (i.e., 0.05 μg TEQ / kg); at the same time, magnetic separation recovers magnetic metals from the waste ash, resulting in low dioxin content, and the flotation concentrate product K2 can be returned to the incinerator for high-temperature reburning to achieve complete dioxin decomposition; and the flotation tailings are subjected to deep flotation removal of heavy metals; specifically, the carrier flotation tailings are subjected to existing mature heavy metal flotation technology to deeply remove heavy metals such as Pb, Cd, Zn, Cu, and Cr, at least removing heavy metals with leaching activity, and finally obtaining purified tailings with no risk of heavy metal pollution and no dioxin residue, which can be directly discharged or used as building material raw materials.

[0030] Example 2

[0031] This embodiment provides a resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration, which is basically the same as that in Embodiment 1, except that the amount of anthracite slime concentrate added in step 2) is 2%, 4%, 6%, and 8% by dry mass, as denoted as group one, two, three, and four in the table below:

[0032] As shown in the table, as the proportion of anthracite slime concentrate increases, the relative amount of collector in the flotation system decreases. Under the same amount of collector, the concentrate yield decreases continuously. This is because the amount of anthracite slime concentrate in the system increases and the adsorption of reagents leads to a reduction in the collector, resulting in a decrease in the flotation product. At the same time, because carbon remains in the flotation tailings, the carbon adsorbing dioxins leads to an increase in the dioxin content of the flotation tailings. Therefore, the amount of anthracite slime concentrate added should be appropriate.

[0033] Comparative Example 1 This comparative example provides a resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration, which is basically the same as that in Example 1, except that the anthracite slime concentrate mentioned in step 2) is replaced with magnetic separation tailings of the same dry weight, that is, the anthracite slime concentrate is not added. The results are as follows:

[0034] The data in the table shows that without the addition of anthracite slime concentrate to the system, dioxins are mainly found on activated carbon, and the particle size becomes even finer after grinding. This results in the carbon removal agent (composite collector) having no selectivity for the extremely fine activated carbon particles, carrying a large amount of fly ash to the surface. Consequently, the concentrate has an extremely low calorific value and no value for recycling. Furthermore, some activated carbon is still not completely removed, causing the tailings to fail to meet the standards.

[0035] Comparative Example 2 This comparative example provides a resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration, which is basically the same as that in Example 1, except that in step 2), grinding is not performed; instead, the magnetic separation tailings are mixed evenly with anthracite slime concentrate. Specifically: 2) Mix the filter cake with anthracite slime concentrate, wherein the amount of anthracite slime concentrate added is 3% of the mass of waste incineration fly ash; add water at a liquid-to-solid mass ratio of 6:1, without co-grinding, only stir thoroughly to make it evenly dispersed; Steps 1) and 3) are the same as in Example 1; The experimental results are as follows:

[0036] As can be seen from the table, although the calorific value of the concentrate is high, the dioxin content in the flotation tailings is far below the emission standard. This indicates that without sufficient mechanical grinding and mixing, it is difficult to achieve the purpose of carrier flotation. A considerable portion of the activated carbon particles did not float to the surface, resulting in dioxin exceeding the standard in the tailings. At the same time, the reduced yield of carbon concentrate indicates that insufficient grinding leads to a larger amount of reagent used, the particle size does not meet the requirements of flotation, and the porosity of the surface also causes a large amount of reagent to be adsorbed, making it difficult to achieve the expected effect.

[0037] Comparative Example 3 This comparative example provides a resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration, which is basically the same as that in Example 1, except that magnetic separation is not performed in step 1), and anthracite slime concentrate is not added in step 3). Specifically: 1) Desalination: Add water to the fly ash from waste incineration at a solid-liquid mass ratio of 1:8, stir and disperse thoroughly, then filter. The filtrate is then treated to remove salts and recover soluble industrial salts such as NaCl and KCl. The filter cake is repeatedly soaked and washed with a small amount of clean water, and the washing water is added to the filtrate. 2) Co-grinding activation: Add water to the above filter cake at a liquid-to-solid mass ratio of 6:1 and grind it so that the mass percentage of the material with a grinding fineness of ≤200 mesh is 88%; 3) Flotation decarbonization and dioxin removal: The slurry after grinding is fed into a flotation machine, and a composite collector is added for flotation at a dosage of 1.89 kg / t. The concentrate product K2 is obtained by flotation; the dioxin content is tested by sampling the flotation tailings. The experimental results are as follows:

[0038] As can be seen from the table, when the magnetic separation step is removed and no carrier flotation is added, i.e., conventional water washing and carbon separation, when faced with high dioxin content in the original waste incineration fly ash, it can only reach the original landfill standard limit of less than 3 μg TEQ / kg, and it is difficult to reach less than 0.05 μg TEQ / kg. Moreover, after removing the magnetic separation step, the dioxin content is even higher than that in Comparative Example 1, indicating that the magnetic metal removed by magnetic separation also carries a small amount of dioxins (this part is used as a smelting raw material, and the dioxin content is not a concern), further proving the rationality and effectiveness of the method of the present invention.

[0039] Comparative Example 4 This comparative example provides a resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration, which is basically the same as that in Example 1, except that the coal slime concentrate mentioned in step 2) is replaced with an equal dry weight of anthracite slime, that is, anthracite slime with an ash content of 56.77% is added. Specifically: 2) Co-grinding activation: Magnetic separation tailings and anthracite slime are mixed in their original form, with the slime added at 3% of the mass of waste incineration fly ash; water is added at a liquid-to-solid mass ratio of 6:1, and co-grinding is performed to achieve a material mass of 88.02% with a grinding fineness ≤200 mesh. The results are as follows:

[0040] The data in the table shows that when anthracite slime concentrate is replaced with the original anthracite slime in the system, the amount of adsorbed carbon is reduced, and adding the same mass of anthracite slime cannot meet the carbon demand, resulting in incomplete dioxin removal. At the same time, the calorific value of K2 in the concentrate is reduced significantly, but the yield does not change much. This is because the slime contains a large amount of extremely fine ash minerals, which become even finer after grinding, resulting in a larger specific surface area for adsorbing flotation reagents. At the same time, it reduces the selectivity of the flotation reagents. Using anthracite slime concentrate can reduce the amount of external materials used and avoid introducing a large amount of ash minerals that adsorb reagents.

[0041] Comparative Example 5 This comparative example provides a resource utilization method for the co-removal of dioxins from waste incineration fly ash by flotation, which is basically the same as that in Example 1, except that step 1) magnetic separation and desalination are omitted, and the fly ash is directly co-ground and flotated with coal slime concentrate. Specifically: 1) Co-grinding activation: Waste incineration fly ash is mixed with anthracite slime concentrate, wherein the amount of anthracite slime concentrate added is 3% of the mass of waste incineration fly ash after removing soluble salts. The subsequent liquid-to-solid ratio and solid mass are also calculated based on the mass of waste incineration fly ash after removing soluble salts plus the mass of coal slime concentrate. Water is added at a liquid-to-solid mass ratio of 6:1 for co-grinding, so that the mass proportion of material with a grinding fineness of ≤200 mesh is 88.02%, which fully activates the particle surface, uniformly disperses the carrier, and destroys the pore structure and agglomeration of waste incineration fly ash, providing a basis for subsequent carrier flotation. 3) Carrier flotation for decarbonization and dioxin removal: The slurry after grinding is fed into the flotation machine, and a composite collector (a mixed collector prepared by diesel oil: white oil: MIBC = 3:1:1) is added for flotation for 5 minutes at a dosage of 1.89 kg / t. The concentrate product K2 is obtained by flotation. The dioxin content is tested by sampling the flotation tailings.

[0042] The results are as follows:

[0043] The data in the table shows that without magnetic separation, some dioxins attached to magnetic minerals cannot be removed. Without salt separation, excessive salt content affects the flotation effect, resulting in an inhibitory effect, reduced flotation yield, and increased flotation reagent dosage. Although the residual dioxin content is low due to the action of anthracite slime concentrate, the expected separation effect is still not achieved. Moreover, it is difficult to recover magnetic products by flotation, resulting in some waste of resources.

[0044] The above embodiments are only used to illustrate the technical solutions of the present invention, and are not intended to limit it. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention, and they should all be covered within the scope of the claims and specification of the present invention.

Claims

1. A method for the resource utilization of waste incineration fly ash carrier flotation for synergistic removal of dioxins, characterized in that, Includes the following steps: 1) Magnetic separation: Add the fly ash from waste incineration to water, stir and disperse it thoroughly, and then perform magnetic separation to obtain magnetic material product K1 and magnetic separation tailings slurry; 2) Desalination: The magnetic separation tailings slurry from step 1) is filtered to obtain desalination filter cake and filtrate; 3) Co-grinding activation: After the desalination filter cake and anthracite slime concentrate are mixed evenly, water is added and co-grinding is carried out; 4) Carrier flotation for decarbonization and dioxin removal: The slurry after grinding is subjected to flotation to obtain concentrate product K2 and flotation tailings.

2. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 1, characterized in that, The solid-liquid ratio of the fly ash from waste incineration to water in step 1) is 1:(5-10).

3. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 1, characterized in that, It also includes desalination of the filtrate from step 2).

4. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 1, characterized in that, The amount of anthracite slime concentrate added in step 3) is 2-10% of the magnetic separation tailings.

5. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 4, characterized in that, The solid-liquid ratio in the grinding process described in step 3) is 5-10:

1.

6. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 1, characterized in that, In step 3), the material mass of the grinding fineness ≤ 200 mesh is > 85%.

7. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 4, characterized in that, The anthracite slime concentrate ash content in step 3) is 10-20%.

8. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 1, characterized in that, The composite collector used in the flotation process described in step 4) is at least one of diesel oil, kerosene, and white oil, and a mixture of at least one of No. 2 oil, 2-octanol, and MIBC.

9. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 4, characterized in that, The flotation described in step 4) is a single flotation, with a flotation time of 3-5 minutes and a reagent dosage of 1-2 kg / t.

10. The resource utilization method for the co-removal of dioxins by flotation of fly ash from waste incineration as described in claim 1, characterized in that, It also includes heavy metal flotation of the flotation tailings in step 4), and deep removal of heavy metals such as Pb, Cd, Zn, Cu, and Cr.

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