A sorting system and method for gasified fly ash

Abstract

The present application relates to a kind of sorting system and method for gasification fly ash, belong to the technical field of gasification fly ash sorting recovery, solve the problem that present technology in gasification fly ash high carbon content, high water content causes its resource utilization problem.The present application includes first wet type rod mill, spiral chute, first thickener, first buffer bucket, first ultrahigh pressure filter and first crusher.The present application is sorted by spiral chute sorting machine, and iron sulfide, iron oxide in material is discharged in advance, so that the product structure to be sorted is scientific and reasonable, improves the stability of subsequent sorting system, and also be conducive to improving product quality;With the powerful dewatering capacity of ultrahigh pressure filtration system, the water content of product meets the requirements;The separation of gasification fly ash multi-component can avoid the influence of multi-component mixture on product quality, and is beneficial to its resource utilization.

Description

Technical Field

[0001] The present invention relates to the technical field of solid waste resource utilization, and in particular to a sorting system and method for gasified fly ash. Background Art

[0002] my country, the world's largest market for coal gasification technology, operates nearly 1,000 gasifiers, consuming over 250 million tons of coal annually. The short residence time of the coal-water slurry and pulverized coal in the gasifier results in incomplete combustion, resulting in unburned carbon content as high as 25-60%. Furthermore, to remove fly ash from the syngas, recycled water scrubbing is used, resulting in a moisture content of 50-70%. The high carbon and moisture content of fly ash significantly impacts its efficient storage, landfill, and resource utilization.

[0003] Common decarbonization methods currently include flotation and spiral chutes. The former, due to the high porosity of gasified fly ash, results in high reagent consumption, significantly increasing economic and environmental costs, making it unsuitable for large-scale application. The latter, due to the small difference in specific gravity between unburned carbon and ash-based materials, results in poor separation efficiency, often failing to produce a high-quality product. Existing dehydration equipment, such as horizontal belt vacuum filter cloth machines, filter presses, and pressure filters, is ineffective for dehydrating gasified fly ash.

[0004] In order to solve the problem that gasification fly ash cannot be utilized as a resource due to its high carbon and water content, it is urgent to develop a gasification fly ash separation process with simple process, wide adaptability and strong processing capacity. Summary of the Invention

[0005] In view of the above analysis, the embodiments of the present invention aim to provide a system and method for sorting gasification fly ash, so as to solve the problem that the existing gasification fly ash cannot be utilized as a resource due to its high carbon and high water content.

[0006] In one aspect, the present invention provides a sorting system for gasification fly ash, comprising a first wet rod mill, a spiral chute, a first concentrator, a first buffer tank, a first ultra-high pressure filter, and a first crusher.

[0007] Furthermore, the spiral chute is provided downstream of the first wet rod mill, the first concentrator is located downstream of the spiral chute, and the first buffer tank is provided downstream of the first concentrator.

[0008] Furthermore, the first ultra-high pressure filter is arranged downstream of the first buffer tank, and the first crusher is arranged downstream of the first ultra-high pressure filter.

[0009] Furthermore, it also includes a second wet rod mill, a second-stage magnetic separator and a third buffer barrel which are arranged in sequence.

[0010] Furthermore, the second-stage magnetic separator is arranged downstream of the second wet rod mill, and the third buffer barrel is arranged downstream of the second-stage magnetic separator.

[0011] Furthermore, the magnetic field strength of the pole surface of the two-stage magnetic separator is 160-480 kA / m.

[0012] Furthermore, after grinding in the first wet rod mill, the particle size range of the product is less than 0.074 mm, accounting for more than 95%, and the particle size range is less than 0.045 mm, accounting for more than 60%.

[0013] Furthermore, the particle size range of the product after grinding in the second wet rod mill is less than 0.038 mm, accounting for more than 95%.

[0014] Furthermore, the feed mass concentration of the spiral chute is 10-35%.

[0015] On the other hand, the present invention provides a method for sorting gasification fly ash, which uses the above-mentioned sorting system for gasification fly ash to perform sorting.

[0016] Compared with the prior art, the present invention can achieve at least one of the following beneficial effects:

[0017] (1) The present invention uses a spiral chute separator to discharge iron sulfides and iron oxides in the material in advance, so that the structure of the product to be sorted is scientific and reasonable, the stability of the subsequent sorting system is improved, and it is also beneficial to improve product quality; with the help of the powerful dehydration capacity of the ultra-high pressure filtration system, the moisture content of the product meets the requirements.

[0018] (2) The present invention avoids the introduction of flotation reagents through gravity separation and magnetic separation. The recyclable magnetic medium is beneficial to cost control and reduced environmental pollution. The short-process continuous coal slime separation process is beneficial to improving the system processing capacity and system stability, while reducing production and investment costs.

[0019] (3) The separation of multiple components of gasification fly ash by the present invention can avoid the influence of multi-component mixing on product quality, which is beneficial to its resource utilization.

[0020] In the present invention, the above-mentioned technical solutions can be combined with each other to achieve more preferred combinations. Other features and advantages of the present invention will be described in the following description, and some advantages will become apparent from the description or be learned through practice of the present invention. The objectives and other advantages of the present invention can be realized and obtained through the contents particularly pointed out in the description and drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] The accompanying drawings are only for the purpose of illustrating particular embodiments and are not to be considered limiting of the present invention. Like reference symbols denote like parts throughout the drawings.

[0022] Figure 1 is a schematic structural diagram of a system for separating gasified fly ash according to a specific embodiment;

[0023] Figure 2 The figure is a flow chart of a method for sorting gasification fly ash according to a specific embodiment.

[0024] Reference numerals:

[0025] 1-First wet rod mill; 2-Spiral chute; 3-First concentrator; 4-First buffer tank; 5-First ultra-high pressure filter; 6-First crusher; 7-Forced mixing tank; 8-First stage magnetic separator; 9-Second concentrator; 10-Second buffer tank; 11-Second ultra-high pressure filter; 12-Second crusher; 13-Second wet rod mill; 14-Second stage magnetic separator; 15-Third buffer tank; 16-Third concentrator; 17-Fourth buffer tank; 18-Third ultra-high pressure filter; 19-Third crusher. DETAILED DESCRIPTION

[0026] The preferred embodiments of the present invention will be described in detail below with reference to the accompanying drawings, wherein the accompanying drawings constitute a part of the present invention and are used together with the embodiments of the present invention to illustrate the principles of the present invention, but are not used to limit the scope of the present invention.

[0027] Example 1

[0028] A specific embodiment of the present invention, as Figure 1 and Figure 2 As shown, a sorting system for gasification fly ash is disclosed, including a first wet rod mill 1, a spiral chute 2, a first concentrator 3, a first buffer tank 4, a first ultra-high pressure filter 5 and a first crusher 6. The spiral chute 2 is arranged downstream of the first wet rod mill 1, the first concentrator 3 is located downstream of the spiral chute 2, the first buffer tank 4 is arranged downstream of the first concentrator 3, the first ultra-high pressure filter 5 is arranged downstream of the first buffer tank 4, and the first crusher 6 is arranged downstream of the first ultra-high pressure filter 5.

[0029] Specifically, the discharge port of the first wet rod mill 1 is connected to the feed port of the spiral chute 2, the first discharge port of the spiral chute 2 is connected to the feed port of the first concentrator 3, the discharge port of the first concentrator 3 is connected to the feed port of the first buffer barrel 4, the discharge port of the first buffer barrel 4 is connected to the feed port of the first ultra-high pressure filter 5, the discharge port of the first ultra-high pressure filter 5 is connected to the feed port of the first crusher 6, and the discharge port of the first crusher 6 outputs iron products.

[0030] During implementation, the gasified fly ash is fed from the feed port of the first wet rod mill 1 and ground in the first wet rod mill 1. The first wet rod mill 1 is used to dissociate the various mineral components (mainly unburned carbon, ash-based substances, and iron-containing minerals) in the gasified fly ash. The separation of the gasified fly ash components can avoid the impact of multi-component mixing on product quality, which is beneficial to its resource utilization. After the ground product flows out of the discharge port of the first wet rod mill 1, it is fed into the spiral chute 2 from the feed port of the spiral chute 2 by gravity for sorting. The iron sulfide, iron oxide and other materials with higher density in the ground product are sorted out. These materials will reduce the loss on ignition of the unburned carbon when entering the unburned carbon, and will increase the loss on ignition of the tail ash and increase the sulfur content in the tail ash when entering the tail ash, affecting its resource utilization. The heavy products in the spiral chute 2 (i.e., materials with higher density, such as iron sulfide and iron oxide) flow out from the first discharge port of the spiral chute 2, enter the first concentrator 3 through the feed port of the first concentrator 3 for concentration, and then enter the first buffer tank 4. After dehydration, the filter cake enters the first crusher 6 for crushing and finally becomes an iron product.

[0031] It should be noted that the loss on ignition refers to the percentage of the mass of the raw material that has lost external moisture by drying it in the temperature range of 105-110°C and burning it for a sufficiently long time under certain high temperature conditions as a percentage of the mass of the original sample.

[0032] Compared with the prior art, the sorting system for gasified fly ash provided in this embodiment uses the spiral chute 2 to discharge the iron fluidized materials and iron oxides in the material in advance, so that the structure of the product to be sorted is scientific and reasonable, the stability of the subsequent sorting system is improved, and it is also beneficial to improve the product quality; with the help of the powerful dehydration capacity of the ultra-high pressure filtration system, the moisture content of the product meets the requirements.

[0033] Preferably, after the raw ore is ground in the first wet rod mill 1, the particle size range of the raw ore is less than 0.074 mm, accounting for more than 95%, and the particle size range of the raw ore is less than 0.045 mm, accounting for more than 60%. The feed mass concentration of the spiral chute 2 is preferably 10-35%.

[0034] The sorting system for gasification fly ash also includes a forced mixing barrel 7, a first-stage magnetic separator 8, a second concentrator 9, a second buffer barrel 10, a second ultra-high pressure filter 11 and a second crusher 12; the forced mixing barrel 7 is arranged downstream of the spiral chute 2, the first-stage magnetic separator 8 is arranged downstream of the forced mixing barrel 7, the second concentrator 9 is arranged downstream of the first-stage magnetic separator 8, the second buffer barrel 10 is arranged downstream of the second concentrator 9, the second ultra-high pressure filter 11 is arranged downstream of the second buffer barrel 10, and the second crusher 12 is arranged downstream of the second ultra-high pressure filter 11.

[0035] Specifically, the second discharge port of the spiral chute 2 is connected to the inlet of the forced stirring barrel 7, the discharge port of the forced stirring barrel 7 is connected to the inlet of the first magnetic separator 8, the tailings outlet of the first magnetic separator 8 is connected to the inlet of the second concentrator 9, the discharge port of the second concentrator 9 is connected to the inlet of the second buffer barrel 10, the discharge port of the second buffer barrel 10 is connected to the inlet of the second ultra-high pressure filter 11, the discharge port of the second ultra-high pressure filter 11 is connected to the inlet of the second crusher 12, and the discharge port of the second crusher 12 outputs the tailings product.

[0036] During implementation, the light products (i.e., materials other than the heavy products) in the spiral chute 2 are discharged from the second discharge port of the spiral chute 2 and enter the forced stirring barrel 7. Nano-magnetite powder is passed through the forced stirring barrel 7. Taking advantage of the fact that the unburned carbon in the gasification fly ash has a large number of pores and strong adsorption, while the ash-based materials have almost no pores and weak adsorption, a large amount of nano-magnetite powder is adsorbed on the unburned carbon. The magnetically activated materials in the forced stirring barrel 7 are discharged from the discharge port of the forced stirring barrel 7 and fed into the feed port of a first-stage magnetic separator 8 for sorting. The tailings from the first-stage magnetic separator 8 are ash-based materials that have not been magnetically activated. This part of the material first enters the second concentrator 9 for concentrating, and then is transported to the second buffer barrel 10. The material discharged from the second buffer barrel 10 is fed into the second ultra-high pressure filter 11 through the feed port of the second ultra-high pressure filter 11 for dehydration. The filter cake formed by the dehydration of the second ultra-high pressure filter 11 is fed into the second crusher 12 for crushing, and the tailing ash product is discharged.

[0037] In this embodiment, gravity separation (spiral chute 2) and magnetic separation are used to avoid the introduction of flotation agents. At the same time, the recyclable magnetic medium is beneficial to cost control and reduction of environmental pollution. Both gravity separation and magnetic separation only require one separation to achieve the desired effect. The short-process continuous slime separation process is beneficial to improving the system processing capacity and system stability, while reducing production and investment costs.

[0038] The sorting system for gasification fly ash also includes a second wet rod mill 13, a second-stage magnetic separator 14 and a third buffer barrel 15. The second wet rod mill 13 is arranged downstream of the first-stage magnetic separator 8, the second-stage magnetic separator 14 is arranged downstream of the second wet rod mill 13, and the third buffer barrel 15 is arranged downstream of the second-stage magnetic separator 14.

[0039] Specifically, the concentrate outlet of the first-stage magnetic separator 8 is connected to the feed port of the second wet rod mill 13, the discharge port of the second wet rod mill 13 is connected to the feed port of the second-stage magnetic separator 14, the concentrate outlet of the second-stage magnetic separator 14 is connected to the feed port of the third buffer barrel 15, and the discharge port of the third buffer barrel 15 is connected to the feed port of the forced stirring barrel 7.

[0040] Preferably, the magnetic field strength of the magnetic pole surface of the first magnetic separator 8 is 72-200 kA / m, and the magnetic field strength of the magnetic pole surface of the second magnetic separator 14 is 160-480 kA / m. The particle size range of the product after grinding in the second wet rod mill 13 is less than 0.038 mm, accounting for more than 95%.

[0041] During implementation, the concentrate output from the concentrate port of the first-stage magnetic separator 8 is magnetically activated unburned carbon. This part of the material enters the second wet rod mill 13 from the feed port of the second wet rod mill 13. The second wet rod mill 13 deeply dissociates and breaks the material entering therein, releasing the nano-magnetite powder adsorbed in the unburned carbon. The unburned carbon that has passed through the deep grinding of the second wet rod mill 13 enters the second-stage magnetic separator 14 for magnetic medium recovery. The magnetically separated concentrate nano-magnetite powder formed by the second-stage magnetic separator 14 enters the third buffer barrel 15 for storage, and the nano-magnetite powder in the third buffer barrel 15 can be transported to the forced stirring barrel 7.

[0042] In this embodiment, the nano-magnetite powder produced by the second-stage magnetic separator 14 can be transported to the forced mixing drum 7 as feed material for the forced mixing drum 7. Taking advantage of the fact that the unburned carbon in the gasification fly ash has a large amount of pores and strong adsorption, while the ash-based material has almost no pores and weak adsorption, a large amount of nano-magnetite powder is adsorbed on the unburned carbon before magnetic separation. The nano-magnetite powder produced subsequently can be used as feed material for the previous step, allowing material recycling and saving raw materials.

[0043] The sorting system for gasification fly ash also includes a third concentrator 16, a fourth buffer tank 17, a third ultra-high pressure filter 18 and a third crusher 19. The third concentrator 16 is located downstream of the second-stage magnetic separator 14, the fourth buffer tank 17 is located downstream of the third concentrator 16, the third ultra-high pressure filter 18 is located downstream of the fourth buffer tank 17, and the third crusher 19 is located downstream of the third ultra-high pressure filter 18.

[0044] Specifically, the tailings outlet of the second-stage magnetic separator 14 is connected to the feed port of the third concentrator 16, the discharge port of the third concentrator 16 is connected to the feed port of the fourth buffer barrel 17, the discharge port of the fourth buffer barrel 17 is connected to the feed port of the third ultra-high pressure filter 18, the discharge port of the third ultra-high pressure filter 18 is connected to the feed port of the third crusher 19, and the third crusher 19 outputs clean coal products.

[0045] During implementation, the magnetic tailings from the second-stage magnetic separator 14 enter the third concentrator 16 for concentrating. The concentrated material enters the fourth buffer barrel 17 from the discharge port of the third concentrator 16 through the feed port of the fourth buffer barrel 17 for storage, and is then transported to the third ultra-high pressure filter 18 for dehydration. The filter cake formed by dehydration in the third ultra-high pressure filter 18 is fed into the third crusher 19 for crushing and output as a clean coal product.

[0046] Preferably, the compaction pressures of the first ultrahigh pressure filter 5 , the second ultrahigh pressure filter 11 and the third ultrahigh pressure filter 18 are all above 20 MPa.

[0047] In this embodiment, gravity and magnetic separation methods are used to avoid the introduction of flotation agents. The recyclable magnetic medium helps control costs and reduce environmental pollution. The short-process continuous coal slime separation process improves system processing capacity and stability while reducing production and input costs.

[0048] In this embodiment, the raw gasification fly ash to be sorted is fed into a first wet rod mill 1 to separate the various mineral components in the gasification fly ash. The ground product flows by gravity into a spiral chute 2 to separate high-density materials such as iron sulfides and iron oxides. These materials enter the unburned carbon, reducing its loss on ignition (LOI). However, entering the tailings ash increases its LOI and sulfur content, affecting its resource utilization. The heavy products in the spiral chute 2 are concentrated and filtered to ultimately become the spiral tail iron product. The light products enter a forced mixing drum 7 filled with nano-magnetite powder. Taking advantage of the high porosity and strong adsorption of the unburned carbon in the gasification fly ash, while the ash-based materials have almost no porosity and weak adsorption, a large amount of nano-magnetite powder is adsorbed into the unburned carbon. The magnetically activated materials in the forced mixing drum 7 enter a first-stage magnetic separator 8 for sorting. The magnetically separated tailings, consisting of ash-based materials that have not been magnetically activated, are concentrated and filtered to ultimately become the tailings product. The first-stage magnetic concentrate, consisting of magnetically activated unburned carbon, enters the second wet rod mill 13 for deep dissociation and pore breaking, releasing the nano-magnetite powder adsorbed in the unburned carbon. The deeply ground unburned carbon enters the second-stage magnetic separator 14 for magnetic medium recovery. The nano-magnetite powder from the magnetic concentrate is stored in a nano-magnetite powder tank. The magnetic tailings are then concentrated and filtered to produce the clean coal product.

[0049] Example 2

[0050] Another specific embodiment of the present invention is as follows Figure 1-Figure 2 As shown, a method for sorting gasified fly ash is disclosed, using the sorting system for gasified fly ash of Example 1, and the steps include:

[0051] Step 1: The mineral components in the gasification fly ash are separated and sorted using a spiral chute 2. The heavy products in the spiral chute 2 are concentrated and filtered to become iron products.

[0052] Specifically, gasified fly ash is fed into the inlet of a first wet rod mill 1 and ground within it. The first wet rod mill 1 is used to separate the various mineral components (primarily unburned carbon, ash-based materials, and iron-containing minerals) within the gasified fly ash. The ground product, after flowing out of the first wet rod mill 1's outlet, is fed into a spiral chute 2 through its inlet for sorting. This separates high-density materials, such as iron sulfides and iron oxides, from the ground product. These materials, when incorporated into the unburned carbon, reduce its loss on ignition (LOI). However, when incorporated into the tail ash, they increase its LOI and sulfur content, impacting its resource utilization. The heavy products in spiral chute 2 flow out of the first outlet of spiral chute 2, pass through the inlet of a first concentrator 3, and are concentrated. After concentration, they enter a first buffer tank 4. After dehydration in an ultrahigh-pressure filter press 5, the filter cake enters a first crusher 6 for crushing, ultimately becoming an iron product.

[0053] This step uses a low-cost spiral separation method to fully dissociate the components in the material. Taking advantage of the fact that the density of iron-containing substances is much greater than that of other substances, the iron-containing substances are separated in advance to prevent this part of the material from affecting the subsequent carbon ash separation.

[0054] Step 2: The light products in the spiral chute 2 enter the forced stirring barrel 7 for magnetic activation, and then enter the first-stage magnetic separator 8 for sorting. The magnetically separated tailings are concentrated and filtered to become tailing ash products.

[0055] Specifically, the light product in the spiral chute 2 is discharged from the second discharge port of the spiral chute 2 and enters the forced stirring barrel 7. Nano-magnetite powder is passed through the forced stirring barrel 7. Taking advantage of the fact that the unburned carbon in the gasification fly ash has a large number of pores and strong adsorption, while the ash-based material has almost no pores and weak adsorption, a large amount of nano-magnetite powder is adsorbed on the unburned carbon. The material magnetically activated in the forced stirring barrel 7 is discharged from the discharge port of the forced stirring barrel 7 and fed into the feed port of a first-stage magnetic separator 8 for sorting. The tailings of the first-stage magnetic separator 8 are ash-based materials that have not been magnetically activated. This part of the material first enters the second concentrator 9 for concentration and is then transported to the second buffer barrel 10. The material discharged from the second buffer barrel 10 is fed into the second ultra-high pressure filter 11 through the feed port of the second ultra-high pressure filter 11 for dehydration. The filter cake formed by the dehydration of the second ultra-high pressure filter 11 is fed into the second crusher 12 for crushing, and the tailing ash product is discharged.

[0056] This step utilizes the characteristics of unburned carbon in gasification fly ash, which has many pores and strong adsorption, and uses nano-magnetite powder to magnetically activate the unburned carbon to make it magnetic, and then uses magnetic separation to separate it. The entire process only requires water and magnetite powder, and the process is simple and environmentally friendly.

[0057] Step 3: The concentrate from the first-stage magnetic separator 8 enters the second wet rod mill 13 for deep dissociation and pore breaking, releasing the nano-magnetite powder adsorbed in the unburned carbon. The deep-ground unburned carbon material enters the second-stage magnetic separator 14 for magnetic medium recovery. The magnetic separation tailings are then concentrated and filtered to produce clean coal.

[0058] Specifically, the concentrate output from the concentrate port of the first-stage magnetic separator 8 is magnetically activated unburned carbon. This part of the material enters the second wet rod mill 13 from the feed port of the second wet rod mill 13. The second wet rod mill 13 deeply dissociates and breaks the material entering therein, releasing the nano-magnetite powder adsorbed in the unburned carbon. The unburned carbon that has been deeply ground in the second wet rod mill 13 enters the second-stage magnetic separator 14 for magnetic medium recovery. The nano-magnetite powder of the magnetically separated concentrate formed by the second-stage magnetic separator 14 enters the third buffer barrel 14 for storage, and the nano-magnetite powder in the third buffer barrel 14 can be transported to the forced stirring barrel 7.

[0059] The magnetic tailings from the second-stage magnetic separator 14 enter the third concentrator 16 for concentrating. The concentrated material is stored in the fourth buffer tank 17 from the discharge port of the third concentrator 16 through the feed port of the fourth buffer tank 17, and then transported to the third ultra-high pressure filter 18 for dehydration. The filter cake formed by dehydration in the third ultra-high pressure filter 18 is fed into the third crusher 19 for crushing and output as a clean coal product.

[0060] This step uses deep grinding to break holes to release the magnetite powder adsorbed in the holes, and then uses magnetic separation to separate the unburned carbon. This process realizes the recovery of magnetic media and helps reduce costs.

[0061] The sorting method for gasification fly ash of this embodiment uses a spiral chute separator to discharge iron sulfides and iron oxides in the material in advance, so that the structure of the product to be sorted is scientific and reasonable, the stability of the subsequent sorting system is improved, and it is also beneficial to improve product quality; with the help of the powerful dehydration capacity of the ultra-high pressure filtration system, the moisture content of the product meets the requirements. The introduction of flotation agents is avoided by gravity separation and magnetic separation, and the recyclable magnetic medium is beneficial to cost control and reduction of environmental pollution. The short-process continuous coal slime sorting process is beneficial to improving the system processing capacity and system stability, while reducing production and investment costs. The separation of multiple components of gasification fly ash can avoid the impact of multi-component mixing on product quality, which is beneficial to its resource utilization.

[0062] The above description is only a preferred specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any changes or substitutions that can be easily thought of by any technician familiar with this technical field within the technical scope disclosed by the present invention should be covered by the scope of protection of the present invention.

Claims

1. A sorting system for gasification fly ash, characterized in that: The invention comprises a first wet rod mill (1), a spiral chute (2), a first concentrator (3), a first buffer tank (4), a first ultra-high pressure filter (5), a first crusher (6), a forced stirring tank (7), a first magnetic separator (8), a second wet rod mill (13), a second magnetic separator (14) and a third buffer tank (15); The spiral chute (2) is arranged downstream of the first wet rod mill (1), and the discharge port of the first wet rod mill (1) is communicated with the feed port of the spiral chute (2); The forced stirring barrel (7) is arranged downstream of the spiral chute (2), the first stage magnetic separator (8) is arranged downstream of the forced stirring barrel (7), the second discharge port of the spiral chute (2) is communicated with the feed port of the forced stirring barrel (7), and the discharge port of the forced stirring barrel (7) is communicated with the feed port of the first stage magnetic separator (8); nano magnetite powder is passed through the forced stirring barrel (7); The second-stage magnetic separator (14) is arranged downstream of the second wet rod mill (13), the third buffer barrel (15) is arranged downstream of the second-stage magnetic separator (14), the second wet rod mill (13) is arranged downstream of the first-stage magnetic separator (8), the concentrate outlet of the first-stage magnetic separator (8) is communicated with the feed port of the second wet rod mill (13), and the discharge port of the second wet rod mill (13) is communicated with the feed port of the second-stage magnetic separator (14).

2. The separation system for gasification fly ash according to claim 1, characterized in that: The first concentrator (3) is located downstream of the spiral chute (2), and the first buffer tank (4) is located downstream of the first concentrator (3).

3. The separation system for gasification fly ash according to claim 2, characterized in that: The first ultra-high pressure filter (5) is arranged downstream of the first buffer tank (4), and the first crusher (6) is arranged downstream of the first ultra-high pressure filter (5).

4. The separation system for gasification fly ash according to claim 1, characterized in that: The magnetic field intensity of the pole surface of the second-stage magnetic separator (14) is 160-480 kA / m.

5. The separation system for gasification fly ash according to claim 1, characterized in that: The particle size of the product after grinding in the first wet rod mill (1) is less than 0.074 mm, accounting for more than 95%, and the particle size is less than 0.045 mm, accounting for more than 60%.

6. The separation system for gasification fly ash according to claim 1, characterized in that: The particle size range of the product after grinding in the second wet rod mill (13) is less than 0.038 mm, accounting for more than 95%.

7. The gasification fly ash sorting system according to any one of claims 1 to 6, characterized in that: The feed mass concentration of the spiral chute (2) is 10-35%.

8. A method for sorting gasified fly ash, characterized in that: The gasification fly ash is sorted using the sorting system for gasification fly ash according to any one of claims 1 to 7.

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