Converter primary flue gas dedusting ash resource utilization treatment system

Abstract

The utility model provides a converter primary flue gas dedusting ash resource utilization treatment system, which comprises a converter primary flue gas purification treatment system and a dedusting ash treatment system which are matched for use, the dedusting ash treatment system receives dedusting ash from the converter primary flue gas purification treatment system, sorts and peels iron powder from the dedusting ash, and collects the iron powder; the fly ash treatment system comprises a multi-stage separation oxidation system and a reduction system which are communicated in sequence, the multi-stage separation oxidation system collects magnetic micro powder in fly ash after separation oxidation, the magnetic micro powder is conveyed into the reduction system to complete the iron powder reduction process, and the obtained iron powder is collected. According to the system, the fly ash is collected by the converter primary flue gas purification treatment system and then delivered to the fly ash treatment system, Fe and oxides thereof contained in the fly ash are converted into Fe powder after separation, oxidation and reduction, the Fe contained in the fly ash is effectively separated, and resource utilization of the converter primary flue gas fly ash is achieved.

Description

TECHNICAL FIELD

[0001] The utility model relates to energy -conserving and environment -friendly equipment field especially relates to a converter primary flue dust removal ash resource utilization treatment system. BACKGROUND

[0002] Converter dust removal ash is produced in the converter blowing process. In the blowing process, iron-containing dust is produced, which enters the dust removal system after the flue and is collected. Because the steelmaking temperature is high, the temperature of the iron-containing dust is high, which can reach 1400 DEG C, and the dust removal system is required to be high. With the development of converter steelmaking production and the improvement of steelmaking process, the corresponding dust removal technology is also continuously developed and improved. There are mainly two kinds of purification and recovery methods of steelmaking flue gas, one is wet dust removal, that is, OG dust removal, and the other is dry dust removal, that is, LT dust removal. The dust removal method does not use a large amount of turbid water to wash the flue gas, but uses an evaporative cooler + electrostatic precipitator + coal gas cooler system.

[0003] The converter dust removal ash contains a high content of iron, TFe > 50%, which is a high-quality iron-containing resource. If it is not utilized, not only the resources are wasted, but also a large amount of land is occupied for stacking, and the environment may be polluted. From the metallurgical point of view, the converter dust removal ash has the characteristics of fine particle size, high iron content and high CaO content. At present, the converter primary dust removal ash treatment technology mainly has the schemes of returning to sintering, returning to ironmaking raw material, pressing into blocks and returning to the converter as a coolant and the like. The elements such as K, Na and Zn in the dust removal ash will have adverse effects on the blast furnace smelting, and the elements such as P and S will have adverse effects on the quality of steel. The internal circulation of the dust removal ash in the steel plant is not only not conducive to the steel production, but also has low added value. CONTENT OF THE UTILITY MODEL

[0004] The utility model solves the technical problem of overcoming the defects in the prior art, and provides a converter primary flue dust removal ash resource utilization treatment system. The composition of the dust removal ash is studied, the Fe contained in the dust removal ash is sorted by using the oxidation-reduction method, and the pure dry method purification treatment of the converter primary flue gas is realized.

[0005] To solve the above technical problems, the utility model adopts the technical scheme that a converter primary flue dust removal ash resource utilization treatment system, including the converter primary flue gas purification treatment system and the dust removal ash treatment system that cooperate and use, the dust removal ash treatment system is connected from the dust removal ash of the converter primary flue gas purification treatment system, and the iron powder is sorted and stripped from the dust removal ash and is collected;

[0006] The dust disposal system comprises a first-stage sorting and oxidizing system, a second-stage sorting and oxidizing system and a reduction system connected in sequence, the first-stage sorting and oxidizing system and the second-stage sorting and oxidizing system collect magnetic micro-powder in the dust after sorting and oxidation, the magnetic micro-powder is transported to the reduction system to complete the iron powder reduction process and collect the obtained iron powder.

[0007] Further, the first-stage sorting and oxidizing system comprises a first-stage micro-powder magnetic sorting device, an oxidizing roasting furnace and a second-stage micro-powder magnetic sorting device connected in sequence, the first-stage micro-powder magnetic sorting device and the second-stage micro-powder magnetic sorting device are both connected with the reduction system at the second output end;

[0008] The input end of the first-stage micro-powder magnetic sorting device is connected with an air flow micro-powder mill, a waste heat recovery device is additionally arranged between the oxidizing roasting furnace and the second-stage micro-powder magnetic sorting device, and the first output end of the second-stage micro-powder magnetic sorting device is connected with a dust collector;

[0009] The second output end of the dust collector supplies tailings to the second-stage sorting and oxidizing system, and the first output end is sequentially connected with a heat exchanger, a fan and a diffusion chimney.

[0010] Further, the second-stage sorting and oxidizing system comprises an air flow micro-powder mill, an oxidizing roasting furnace, a waste heat recovery device, a micro-powder magnetic sorting device, a dust collector, a heat exchanger, a fan and a diffusion chimney connected in sequence, and the second output end of the micro-powder magnetic sorting device is connected with the reduction system;

[0011] The second-stage sorting and oxidizing system is at least one group, and the second output end of the dust collector is connected with any one of the group or the next group of air flow micro-powder mills.

[0012] Further, the micro-powder magnetic sorting device comprises a flue gas passage fixedly arranged in the vertical direction, a plurality of sorting components fixedly arranged close to the outer edge of the flue gas passage, the sorting components are composed of a magnetic rotating disc component and a discharge chute, the magnetic rotating disc component is fixedly arranged above the discharge chute, a cleaning device is fixedly arranged in the discharge chute, the cleaning device can contact the surface of the magnetic rotating disc, a plurality of the magnetic rotating discs are coaxially fixed on a rotating drum, and the rotating drum is driven by a driving device.

[0013] Further, the micro-powder magnetic sorting device comprises a flue gas passage fixedly arranged in the vertical direction, a plurality of sorting components fixedly arranged close to the outer edge of the flue gas passage, the sorting components are composed of a magnetic rotating disc component and a discharge chute, the magnetic rotating disc component is fixedly arranged above the discharge chute, a cleaning device is fixedly arranged in the discharge chute, the cleaning device can contact the surface of the magnetic rotating disc, a plurality of the magnetic rotating discs are coaxially fixed on a rotating drum, and the rotating drum is driven by a driving device.

[0014] A magnetic rod frame is arranged on the outer surface of the smoke inlet cavity, and a plurality of magnetic rods are fixedly arranged on the side of the magnetic rod frame facing the smoke inlet cavity, and the magnetic rod frame is rotatably fixed on the outer surface of the smoke inlet cavity.

[0015] Further, the reduction system comprises a reduction roaster, a flue gas filtration and purification device, a waste heat recovery device, a heat exchanger, a fan and a diffusion chimney connected in sequence, the reduction roaster receives the magnetic micro-powder from the primary and secondary sorting oxidation systems and completes the reduction process of the magnetic micro-powder.

[0016] Further, the flue gas filtration and purification device comprises a dust removal shell and a pneumatic conveying device fixedly arranged below the dust removal shell for conveying dust removal ash.

[0017] An air inlet and an air outlet are arranged on the dust removal shell, an air inlet box is fixedly arranged inside the dust removal shell along the length direction of the air inlet, a plurality of axial cyclone sub-units are fixedly arranged in the air inlet box, and a blowing assembly is fixedly arranged above the axial cyclone sub-units; an evaporator assembly is fixedly arranged below the air inlet box.

[0018] Further, the axial cyclone sub-unit comprises a separation cavity fixedly arranged on the bottom plate of the air inlet box and a gas guide assembly fixedly arranged on the top plate of the air inlet box.

[0019] The width of the gas guide assembly is smaller than the width of the side of the separation cavity close to the gas guide assembly, the gas guide assembly and the separation cavity are located on the same axis, the lower end of the gas guide assembly is fixedly embedded with the upper surface of the separation cavity, and the gas guide assembly and the separation cavity are through.

[0020] The gas guide assembly comprises a gas guide sleeve and a ceramic fiber filter tube fixedly arranged in the gas guide sleeve, the gas guide sleeve is a hollow through structure, and a gap is arranged at the upper end of the gas guide sleeve for embedding and fixing the ceramic fiber filter tube; the ceramic fiber filter tube comprises a rigid framework, a plurality of air holes are arranged on the rigid framework, the outer edge of the rigid framework is covered with a ceramic fiber membrane, and a baffle is fixedly arranged at the upper end of the ceramic fiber filter tube.

[0021] Further, a uniform unloading device is arranged in the dust removal shell, the uniform unloading device comprises a spout section fixedly arranged in the dust removal shell with equal gaps, a bottom support plate is fixedly arranged below the spout section at a certain distance from the gap area, and a nozzle is fixedly arranged at the midpoint of the bottom support plate.

[0022] Further, the converter primary flue gas purification treatment system comprises a converter and a vaporization cooling flue communicated with the output end of the converter, the output end of the vaporization cooling flue is sequentially communicated with a multi-stage flue gas filtration and purification device, a waste heat recovery device, a heat exchanger, a fan and a switching valve, the output end of the switching valve is respectively communicated with a gas tank and a diffusion chimney.

[0023] Compared with the prior art, the beneficial effects of the utility model include:

[0024] 1) Collecting dust removal ash by the converter primary flue gas purification treatment system and handing it over to the dust removal ash treatment system, converting Fe and its oxides contained in the dust removal ash into Fe powder by separation and oxidation reduction, effectively separating Fe contained in the dust removal ash, realizing resource utilization of the converter primary flue gas dust removal ash, separating Fe and Fe3O4 in the dust removal ash in the process of treating the dust removal ash, converting FeO, FeO2 and Fe2O3 into Fe and Fe3O4 by oxidation, using Fe as a reducing agent in the reduction process, not involving additional additive addition, not affecting the dust removal ash itself, and simultaneously realizing effective recovery of waste heat;

[0025] 2) By applying the flue gas filtration and purification device in the converter primary flue gas purification treatment system and the reduction system, the ultra-high temperature flue gas is subjected to ultra-clean filtration treatment by the ceramic fiber filter pipe arranged in the center of each cyclone of the axial cyclone, the outlet concentration of the flue gas is less than 5-10 mg / Nm3, the impact and wear of the dust in the ultra-high temperature flue gas on the waste heat boiler are avoided, the dust in the ultra-high temperature flue gas is prevented from gathering, blocking and scaling on the heat exchange surface of the waste heat boiler, the stability and safety of the entire ultra-high temperature flue gas purification filtration and full waste heat recovery system are improved, the high-temperature composite phase change heat storage material is used to form the bottom plate of the air inlet tank, the separation cavity of each axial cyclone, the air guide sleeve of each axial cyclone, the top plate of the air inlet tank and the rigid framework of the ceramic fiber filter pipe, so that the flue gas filtration and purification device has the function of the heat accumulator, the heat energy of the ultra-high temperature flue gas is stored and released by the high-temperature composite phase change heat storage device in a certain ultra-high temperature section, the contradiction between heat supply and demand in time and intensity is solved, and the ultra-high temperature flue gas filtration and purification device basically operates in a relatively constant ultra-high temperature range;

[0026] 3) The pure dry dust removal process technology is adopted, the consumption of water and steam in the converter primary flue gas purification treatment process is "0", the converter, the converter primary flue gas full waste heat recovery, the clean dry coal gas recovery (the heat value of the coal gas is improved), the flue gas ultra-low emission (the emission flue gas dust content is less than or equal to 5-10 mg / Nm 3), avoids secondary pollution, and simultaneously creates favorable conditions for secondary resource utilization treatment of the converter primary dust removal ash. BRIEF DESCRIPTION OF DRAWINGS

[0027] The disclosure of the present application will be explained with reference to the drawings. It should be appreciated that the drawings are for illustrative purposes only and are not intended to limit the scope of protection of the present application. In the drawings, the same reference numerals are used to refer to the same components. Among them:

[0028] Figure 1 The overall structure of the converter primary flue gas dust removal ash resource utilization treatment system is schematically shown;

[0029] Figure 2 The overall structure of the dust removal ash treatment system is schematically shown;

[0030] Figure 3 The overall structure of the first-stage separation oxidation system is schematically shown;

[0031] Figure 4 The overall structure of the second-stage separation oxidation system is schematically shown;

[0032] Figure 5 The cross-sectional structure of the multi-wheel disc piece type fine powder magnetic separation device is schematically shown;

[0033] Figure 6 The cross-sectional structure of the magnetic rotating disc assembly is schematically shown;

[0034] Figure 7 The cross-sectional structure of the magnetic rod type fine powder magnetic separation device is schematically shown;

[0035] Figure 8 The overall structure of the reduction system is schematically shown;

[0036] Figure 9 The cross-sectional structure of the flue gas filtration and purification device is schematically shown;

[0037] Figure 10 The cross-sectional structure of the axial cyclone is schematically shown;

[0038] Figure 11 The cross-sectional structure of the gas guide assembly is schematically shown;

[0039] Figure 12 The cross-sectional structure of the gas guide sleeve is schematically shown;

[0040] Figure 13 The cross-sectional structure of the ceramic fiber filter tube is schematically shown;

[0041] Figure 14 The local enlarged structure of the uniform discharging device is schematically shown;

[0042] Figure 15 The overall structure of the converter primary flue gas purification treatment system is schematically shown.

[0043] Reference numerals in the drawing:

[0044] 1. Converter primary flue gas purification treatment system, 2. Dust ash treatment system, 3. First-stage separation oxidation system, 4. Second-stage separation oxidation system, 5. Reduction system;

[0045] 11. Vaporization cooling flue, 12. Switching valve, 13. Gas holder;

[0046] 31. Airflow micro-powder mill, 32. Micro-powder magnetic separation device, 33. Oxidation roasting furnace, 34. Waste heat recovery device, 35. Dust collector, 36. Heat exchanger, 37. Fan, 38. Diffusion chimney;

[0047] 51. Reduction roasting furnace, 52. Flue gas filtration purification device;

[0048] 521. Dust removal shell, 522. Pneumatic conveying device, 523. Air inlet box, 524. Axial cyclone, 525. Injection assembly, 526. Evaporator assembly, 527. Uniform unloading device;

[0049] 5241. Separation cavity, 5242. Air guide sleeve, 5243. Ceramic fiber filter tube, 5244. Rigid framework, 5245. Vent hole, 5246. Ceramic fiber membrane;

[0050] 5251. Pulse injection pipe, 5252. Gas storage bag, 5253. Pulse injection solenoid valve;

[0051] 5271. Slide pipe section, 5272. Bottom support plate, 5273. Nozzle;

[0052] 32a-1. Flue dust channel, 32a-2. Magnetic rotating disc assembly, 32a-3. Unloading groove, 32a-4. Rotating drum, 32a-5. Driving device;

[0053] 32b-1. Flue gas inlet cavity, 32b-2. Shunt cone shell, 32b-3. Dust outlet cavity, 32b-4. Flue gas outlet cavity, 32b-5. Magnetic rod holder, 32b-6. Magnetic rod. DETAILED DESCRIPTION

[0054] It is easy to understand that according to the technical scheme of the present application, a person skilled in the art can propose a plurality of structure modes and implementation modes which can be replaced with each other without changing the essential spirit of the present application. Therefore, the following specific embodiments and drawings are only exemplary descriptions of the technical scheme of the present application, and should not be regarded as the whole or regarded as the limitation or restriction of the technical scheme of the present application.

[0055] Figure 1 The overall structure of the converter primary flue dust resource utilization treatment system is shown schematically, and a converter primary flue dust resource utilization treatment system as shown in Figure 1 The converter primary flue gas purification treatment system 1 directly receives the flue gas output from the converter steelmaking process, and adsorbs and collects impurities in the flue gas to form dust, and the treated flue gas completes waste heat recovery and can be selectively directly discharged or stored in the gas tank 13; the aforementioned dust enters the dust treatment system 2, which contains Fe, FeO, FeO2, Fe2O3, and Fe3O4 particles with different particle sizes and cannot directly obtain Fe particles, so oxidation and reduction reactions are required to prepare the mixed particles to convert FeO, FeO2, Fe2O3, and Fe3O4 particles into Fe particles, and then the Fe powder is recovered.

[0056] Figure 2 The overall structure of the dust treatment system is shown schematically, as shown in Figure 2 The dust treatment system 2 includes a first-stage selection oxidation system 3, a second-stage selection oxidation system 4, and a reduction system 5 in sequence, the first-stage selection oxidation system 3 and the second-stage selection oxidation system 4 preliminarily separate the magnetic Fe and Fe3O4 particles (i.e., magnetic fine powder) in the dust, and then apply oxidation reaction, under a process temperature of T < 570°C, CO + O2 is introduced to oxidize the mixed particles, so that the FeO, FeO2, and Fe2O3 iron oxide fine powder particles are oxidized to Fe3O4 (with magnetism), which creates conditions for separating FeO, FeO2, and Fe2O3 iron oxide fine powder particles from the fine powder, and then secondary selection can separate most of the Fe-containing particles. The second-stage selection oxidation system 4 performs secondary oxidation selection to basically convert the Fe contained in the dust into Fe and Fe3O4 particles, and then enters the reduction system 5, under a furnace temperature condition of 570°C < T10 < 1000°C, CO + H2 gas is introduced to reduce the magnetic fine powder particles such as Fe and Fe3O4 into reduced iron powder and collect it to complete the recovery process of the Fe powder in the dust, and realize the resource utilization of the dust.

[0057] Figure 3 The overall structure of the first-stage selection oxidation system is shown schematically, as shown in Figure 3As shown, the aforementioned first-stage sorting oxidation system 3 comprises a first-stage micro-powder magnetic sorting device 32, an oxidation roaster 33 and a second-stage micro-powder magnetic sorting device 32 connected in sequence, and the first-stage micro-powder magnetic sorting device 32 and the second output end of the second-stage micro-powder magnetic sorting device 32 are both communicated with the reduction system 5. The input end of the first-stage micro-powder magnetic sorting device 32 is communicated with the jet micro-powder mill 31, and a waste heat recovery device 34 is additionally arranged between the oxidation roaster 33 and the second-stage micro-powder magnetic sorting device 32 for recovering the waste heat of the dust removal ash, and the first output end of the second micro-powder magnetic sorting device 32 is communicated with a dust collector 35; the second output end of the dust collector 35 supplies tailings to the second-stage sorting oxidation system 4, and the first output end thereof is sequentially connected with a heat exchanger 36, a fan 37 and a diffusion chimney 38.

[0058] The first-stage sorting process is specifically as follows:

[0059] (1) Jet breaking / sorting

[0060] Firstly, the hot ash in the ash hopper of the converter primary pure dry purification treatment system ultra-high temperature flue gas filtration purification device 52 is sent into the jet micro-powder mill 31 through high-pressure nitrogen for breaking / sorting. The jet micro-powder mill 31 peels off the surfaces of Fe, FeO, FeO2, Fe2O3 and Fe3O4 particles in the converter primary dust removal ash, removes the impurities on the surfaces of Fe, FeO, FeO2, Fe2O3 and Fe3O4 particles, sorts out micro-powder materials with a particle size of D50≤10 μm, and increases the surface area and activity of the micro-powder.

[0061] (2) First-stage micro-powder magnetic sorting

[0062] A first-stage micro-powder magnetic sorting device is arranged on the conveying air pipe for conveying the micro-powder materials with a particle size of D50≤10 μm broken / sorted in the previous process to the next process, so as to sort out the Fe and Fe3O4 particles with magnetism in the micro-powder and send them to the reduction process to make reduced iron powder.

[0063] Mechanism of the micro-powder magnetic sorting device arranged on the flue:

[0064] Fe and Fe3O4 micro-powder particles can be dissociated at ≤30-50 μm. At this particle size, the Fe and Fe3O4 micro-powder particles cannot be separated from other mineral micro-powder particles by using traditional magnetic separation equipment, because the Fe and Fe3O4 micro-powder particles and other mineral micro-powder particles in the micro-powder are magnetically agglomerated and electrostatically adsorbed under the action of a strong magnetic field at this particle size of the micro-powder, and cannot be effectively separated. The micro-powder of the converter dust is processed by a full dry method, which requires that the Fe and Fe3O4 micro-powder particles and other mineral micro-powder particles in the micro-powder be separately dispersed in a gas (nitrogen or air) so that the Fe and Fe3O4 micro-powder particles can be effectively separated under the action of a magnetic field.

[0065] (3) Oxidation

[0066] A set of oxidation roasting furnace 33 is provided. The micro-powder after the first stage of micro-powder magnetic separation is sent into the powder roasting furnace, CO+O2 is introduced at a process temperature of T<570 ℃, and the micro-powder is oxidized, so that the FeO, FeO2, and Fe2O3 iron oxide micro-powder particles are oxidized into Fe3O4 (with magnetism), thereby creating conditions for separating the FeO, FeO2, and Fe2O3 iron oxide micro-powder particles from the micro-powder.

[0067] The oxidation reaction of this process is as follows:

[0068] At a temperature of T<570 ℃

[0069] Fe2O3+ 3CO— 加热 —> Fe3O4+ 3CO2

[0070] Fe2O3+ 4FeO— 加热 —> Fe + Fe3O4

[0071] (4) Cooling

[0072] A set of finned heat pipe waste heat recovery device 34 (also as the waste heat recovery device 34) is provided after the oxidation roasting furnace 33. In order to ensure that the Fe3O4 micro-powder particles have magnetism, the flue dust must be cooled to a certain extent to ensure that the Fe3O4 micro-powder particles have magnetism.

[0073] (5) Second stage of micro-powder magnetic separation

[0074] A set of second stage of micro-powder magnetic separation device is provided on the conveying air pipe between the finned heat pipe waste heat recovery device 34 and the high-temperature-resistant ultra-low emission pulse jet bag / soft metal membrane filter cartridge dust collector 35, so as to separate the Fe and Fe3O4 micro-powder particles with magnetism from the micro-powder and send them to the reduction process to make reduced iron powder.

[0075] (6) Exhaust gas purification treatment

[0076] A high-temperature resistant, ultra-low emission pulse-jet bag / flexible metal membrane cartridge dust collector 35 is installed after the second-stage micro-powder magnetic separator to filter and purify the exhaust gas dust after the second-stage micro-powder magnetic separation, ensuring that the exhaust dust content is ≤5~10mg / Nm³. 3 The collected tail powder is sent to the secondary sorting process for further sorting.

[0077] Figure 4 The schematic diagram illustrates the overall structure of the two-stage sorting oxidation system, such as... Figure 4 As shown, the aforementioned secondary sorting oxidation system 4 includes, in sequence, an airflow micro-powder mill 31, an oxidation roasting furnace 33, a waste heat recovery device 34, a micro-powder sorting device, a dust collector 35, a heat exchanger 36, a fan 37, and a venting chimney 38. The second output end of the micro-powder magnetic sorting device 32 is connected to the reduction system 5. That is, compared with the primary sorting oxidation system 3, the secondary sorting oxidation system 4 does not require a magnetic separation process for the micro-powder from the airflow micro-powder mill 31 before the oxidation process. Therefore, compared with the primary sorting oxidation system 3, it lacks a micro-powder sorting device located between the airflow micro-powder mill 31 and the oxidation roasting furnace 33. The rest of the structure is completely the same as the primary sorting oxidation system 3. In the secondary sorting process, it only lacks the first-stage micro-powder magnetic sorting process as in the primary sorting process. The rest of the process is completely the same as the primary sorting process.

[0078] It is worth noting that the second output end of the dust collector 35 in the secondary sorting oxidation system 4 can be connected to the input end of the airflow micro powder mill 31 to circulate the secondary sorting process and completely convert FeO, FeO2 and Fe2O3 in the dust into magnetic micro powder. In another embodiment, multiple sets of secondary sorting oxidation systems 4 can be set up, and the second output end of the previous set of secondary sorting oxidation systems 4 can be connected to the airflow micro powder mill 31 of the next set of secondary sorting systems. However, this embodiment requires multiple sets of secondary sorting oxidation systems 4, which places too much space requirements on the system.

[0079] The micro powder magnetic separation device 32 involved in the aforementioned primary separation oxidation system 3 and secondary separation oxidation system 4 can be a multi-wheel disc type or a magnetic rod type. The micro powder magnetic separation device 32 will be described in detail below.

[0080] Figure 5 The schematic diagram shows a cross-sectional view of a multi-wheel disc-type micro-powder magnetic separator, such as... Figure 5As shown in the figure, a kind of fine powder magnetic separator (multi-wheel disc piece) includes along vertical fixedly arranged with smoke channel 32a-1, close to the outer edge of smoke channel 32a-1 Fixedly arranged with several sorting components, sorting components are composed of magnetic rotating disc component 32a-2 and discharge chute 32a-3, magnetic rotating disc component 32a-2 is fixedly arranged in the upper of discharge chute 32a-3, cleaning device is fixedly arranged in discharge chute 32a-3, cleaning device can be contacted with the surface of magnetic rotating disc, wherein magnetic rotating disc only has partial area with magnetism, such as the upper half area of magnetic rotating disc has magnetism, then magnetic rotating disc only has the magnetic area and can adsorb magnetic fine powder, and when the magnetic area rotates to the cleaning device area, cleaning device is contacted with the surface of the magnetic area, so that the magnetic fine powder adsorbed on the magnetic area is scraped off, the scraped magnetic fine powder falls into discharge chute 32a-3, thereby completing the collection process of magnetic fine powder.

[0081] Figure 6 As shown in the figure, the cross-sectional structure of magnetic rotating disc component is schematically shown, Figure 6 As shown in the figure, the aforementioned magnetic rotating disc can be multiple, multiple magnetic rotating discs are coaxially fixed on the rotating drum 32a-4 to form magnetic rotating disc component, and the rotating drum 32a-4 is driven to rotate by driving device 32a-5 to drive the magnetic rotating disc located thereon to rotate coaxially.

[0082] In order to make the adsorption of magnetic rotating disc for magnetic fine powder in smoke more complete, shunt device is fixedly arranged in smoke channel 32a-1, for shunting smoke channel 32a-1 into multiple smoke channels 32a-1 branch with smaller diameter, multiple groups of magnetic rotating discs are arranged on each smoke channel 32a-1 branch to complete the adsorption of magnetic fine powder, the content of magnetic fine powder contained in the shunted smoke can be obviously reduced, and multiple groups of magnetic rotating discs are arranged to adsorb, which can maximize the adsorption effect of magnetic fine powder in the passing smoke.

[0083] Figure 7 As shown in the figure, the cross-sectional structure of magnetic rod type fine powder magnetic separation device is schematically shown, Figure 7As shown, a kind of fine powder magnetic separator (magnetic rod type) includes smoke inlet cavity 32b-1, fixedly arranged with shunt conical shell 32b-2 in smoke inlet cavity 32b-1, after smoke gas enters smoke inlet cavity 32b-1 from the smoke inlet of smoke inlet cavity 32b-1, complete shunt process under the action of the tip of shunt conical shell 32b-2, because shunt conical shell 32b-2 is fixedly arranged in the middle position of smoke inlet cavity 32b-1, after shunt, smoke gas will be close to the side wall of smoke inlet cavity 32b-1 and flow;Fixedly arranged with dust outlet cavity 32b-3 below smoke inlet cavity 32b-1, fixedly arranged with smoke outlet cavity 32b-4 below shunt conical shell 32b-2, smoke outlet cavity 32b-4 is located in the middle position of smoke inlet cavity 32b-1, and dust outlet cavity 32b-3 is arranged around the aforementioned smoke outlet cavity 32b-4, for cooperating with the shunt flow mode of smoke gas, the upper segment of the aforementioned smoke outlet cavity 32b-4 extends into the lower end of shunt conical shell 32b-2, so that the smoke gas entering smoke inlet cavity 32b-1 is first flowed along the edge of smoke inlet cavity 32b-1 under the action of shunt conical shell 32b-2, and then output from smoke outlet cavity 32b-4 in the lower end of shunt conical shell 32b-2.

[0084] Based on the outer surface of the aforementioned smoke inlet cavity 32b-1, magnetic rod holder 32b-5 is arranged, and a plurality of magnetic rods 32b-6 are fixedly arranged on the side of magnetic rod holder 32b-5 facing smoke inlet cavity 32b-1, for example, smoke inlet cavity 32b-1 is cylindrical structure, and magnetic rod holder 32b-5 is annular structure matched with the outer edge of cylindrical structure, so as to be closely attached to the outer edge surface of smoke inlet cavity 32b-1, and the aforementioned magnetic rods 32b-6 are in close contact with the outer edge surface of smoke inlet cavity 32b-1, magnetic rod holder 32b-5 is rotatably fixedly arranged on the outer surface of smoke inlet cavity 32b-1, specifically, a fixed point is provided on the outer edge surface of smoke inlet cavity 32b-1, magnetic rod holder 32b-5 is fixed with the fixed point by a column, so that magnetic rod holder 32b-5 can rotate around the fixed point, and a telescopic component such as air cylinder is vertically arranged above the smoke inlet of smoke inlet cavity 32b-1, the side of magnetic rod holder 32b-5 away from smoke inlet cavity 32b-1 is an inverted triangle, and the corner of the inverted triangle away from smoke inlet cavity 32b-1 is fixed with the aforementioned telescopic component, to drive the corner to move up and down, so that magnetic rod holder 32b-5 can rotate around the aforementioned fixed point.

[0085] When the magnetic rod holder 32b-5 is in close contact with the side of the smoke inlet cavity 32b-1, the magnetic force of the magnetic rod 32b-6 located thereon can act on the smoke flowing through the smoke inlet cavity 32b-1 and adsorb the magnetic micro-powder located therein onto the side wall of the smoke inlet cavity 32b-1. After the smoke is completely output, the magnetic rod holder 32b-5 is moved away from the smoke inlet cavity 32b-1, and the magnetic micro-powder adsorbed onto the inner wall of the smoke inlet cavity 32b-1 can fall into the dust outlet cavity 32b-3 under the action of gravity, thereby completing the collection of the magnetic micro-powder.

[0086] The first-stage micro-powder magnetic separation device 32 and the second-stage micro-powder magnetic separation device 32 in the first-stage separation and oxidation system 3 and the micro-powder magnetic separation device 32 in the second-stage separation and oxidation system 4 can be selected from any one of the multi-disc micro-powder magnetic separation device 32 or the magnetic rod holder 32b-5 micro-powder magnetic separation device 32.

[0087] Figure 8 The overall structure of the reduction system is schematically shown, and the following will be described in combination with Figure 8 The reduction system 5 will be specifically described. The reduction system 5 includes, in sequence, a reduction roaster 51, a smoke filtration and purification device 52, a waste heat recovery device 34, a heat exchanger 36, a fan 37 and a diffusion chimney 38. The reduction roaster 51 receives the magnetic micro-powder from the first-stage separation and oxidation system 3 and the second-stage separation and oxidation system 4 and completes the reduction process of the magnetic micro-powder. The preparation of the reduced Fe powder is specifically as follows:

[0088] The Fe and Fe3O4 and other magnetic micro-powder particles separated by the micro-powder magnetic separation in the above first-stage / second-stage separation process are sent into the reduction roaster 51. Under the condition of a furnace temperature of 570℃<T10<1000℃, CO+H2 gas is introduced to reduce the Fe and Fe3O4 and other magnetic micro-powder particles into reduced iron powder. The reduced iron powder is collected by the ultra-high-temperature smoke filtration and purification device 52, cooled and then packaged and transported.

[0089] The reduction reaction of this process is as follows:

[0090] 570℃<T<1000℃

[0091] ① Reduction with CO:

[0092] Fe3O4+4CO— 加热 —→3Fe+4CO2

[0093] ② Reduction with H2:

[0094] Fe3O4+4H2— 加热 —→3Fe+4H2O

[0095] Figure 9 schematic cross-sectional view of the flue gas filtering and purifying device is shown in FIG. 2, and a schematic cross-sectional view of the axial cyclone is shown in FIG. 3. Figure 9 As shown in the drawings, the flue gas filtering and purifying device 52 located in the aforementioned reduction system 5 comprises a dust removal shell 521 and a pneumatic conveying device 522 fixedly arranged below the dust removal shell 521 for conveying dust removal ash; an air inlet and an air outlet are formed on the dust removal shell 521, an air inlet box 523 is fixedly arranged inside the dust removal shell 521 along the length direction of the air inlet, a plurality of axial cyclones 524 are fixedly arranged in the air inlet box 523, a blowing assembly 525 is fixedly arranged above the axial cyclones 524, and an evaporator assembly 526 is fixedly arranged below the air inlet box 523. The aforementioned blowing assembly 525 comprises a pulse blowing pipe 5251 and a gas storage bag 5252 for supplying gas to the pulse blowing pipe 5251, a pulse blowing electromagnetic valve 5253 is fixedly arranged between the pulse blowing pipe 5251 and the gas storage bag 5252 for regulating the blowing process, the aforementioned gas storage bag 5252 is in communication with the nitrogen source of the pneumatic conveying device 522, that is, the nitrogen stored in the gas storage bag 5252 is the same as the nitrogen of the pneumatic conveying device 522, and the aforementioned pulse blowing pipe 5251 can be multiple, and a single pulse blowing pipe 5251 can complete the blowing process of multiple axial cyclones 524.

[0096] Figure 10 schematic cross-sectional view of the flue gas filtering and purifying device is shown in FIG. 2, and a schematic cross-sectional view of the axial cyclone is shown in FIG. 3. Figure 10 As shown in the drawings, the flue gas filtering and purifying device 52 located in the aforementioned reduction system 5 comprises a dust removal shell 521 and a pneumatic conveying device 522 fixedly arranged below the dust removal shell 521 for conveying dust removal ash; an air inlet and an air outlet are formed on the dust removal shell 521, an air inlet box 523 is fixedly arranged inside the dust removal shell 521 along the length direction of the air inlet, a plurality of axial cyclones 524 are fixedly arranged in the air inlet box 523, a blowing assembly 525 is fixedly arranged above the axial cyclones 524, and an evaporator assembly 526 is fixedly arranged below the air inlet box 523. The aforementioned blowing assembly 525 comprises a pulse blowing pipe 5251 and a gas storage bag 5252 for supplying gas to the pulse blowing pipe 5251, a pulse blowing electromagnetic valve 5253 is fixedly arranged between the pulse blowing pipe 5251 and the gas storage bag 5252 for regulating the blowing process, the aforementioned gas storage bag 5252 is in communication with the nitrogen source of the pneumatic conveying device 522, that is, the nitrogen stored in the gas storage bag 5252 is the same as the nitrogen of the pneumatic conveying device 522, and the aforementioned pulse blowing pipe 5251 can be multiple, and a single pulse blowing pipe 5251 can complete the blowing process of multiple axial cyclones 524.

[0097] Figure 11 schematic cross-sectional view of the flue gas filtering and purifying device is shown in FIG. 2, and a schematic cross-sectional view of the axial cyclone is shown in FIG. 3. Figure 11 As shown in the drawings, the flue gas filtering and purifying device 52 located in the aforementioned reduction system 5 comprises a dust removal shell 521 and a pneumatic conveying device 522 fixedly arranged below the dust removal shell 521 for conveying dust removal ash; an air inlet and an air outlet are formed on the dust removal shell 521, an air inlet box 523 is fixedly arranged inside the dust removal shell 521 along the length direction of the air inlet, a plurality of axial cyclones 524 are fixedly arranged in the air inlet box 523, a blowing assembly 525 is fixedly arranged above the axial cyclones 524, and an evaporator assembly 526 is fixedly arranged below the air inlet box 523. The aforementioned blowing assembly 525 comprises a pulse blowing pipe 5251 and a gas storage bag 5252 for supplying gas to the pulse blowing pipe 5251, a pulse blowing electromagnetic valve 5253 is fixedly arranged between the pulse blowing pipe 5251 and the gas storage bag 5252 for regulating the blowing process, the aforementioned gas storage bag 5252 is in communication with the nitrogen source of the pneumatic conveying device 522, that is, the nitrogen stored in the gas storage bag 5252 is the same as the nitrogen of the pneumatic conveying device 522, and the aforementioned pulse blowing pipe 5251 can be multiple, and a single pulse blowing pipe 5251 can complete the blowing process of multiple axial cyclones 524. Figure 12 Figure 12 ​As shown, the air guide sleeve 5242 has a hollow through structure. A notch is provided at the top of the air guide sleeve 5242 for the ceramic fiber filter tube 5243 to be fitted and fixed. A convex ring is provided on the outer edge surface, so that the air guide sleeve 5242 can be inserted from the top plate of the air inlet box 523. The upper end of the air guide sleeve 5242 is limited to the top plate of the air inlet box 523 by the convex ring provided on its outer edge surface.

[0098] Figure 13 The schematic diagram shows the cross-sectional structure of the ceramic fiber filter tube, such as Figure 13 As shown, the aforementioned ceramic fiber filter tube 5243 includes a rigid frame 5244. A plurality of ventilation holes 5245 are provided on the rigid frame 5244 along the width direction of the rigid frame 5244. A ceramic fiber membrane 5246 is wrapped around the outer edge of the rigid frame 5244. A baffle is fixedly provided at the upper end of the rigid frame 5244. The rigid frame 5244 can be directly inserted into the air guide sleeve 5242 through the notch provided at the top of the air guide sleeve 5242. The baffle limits the upper end of the ceramic fiber filter tube 5243 to the upper end of the air guide sleeve 5242, thereby fixing the ceramic fiber filter tube 5243 in the aforementioned air guide sleeve 5242.

[0099] Ultra-high temperature flue gas is ultra-cleaned by setting ceramic fiber filter tubes 5243 in the central air guide sleeves 5242 of each axial cyclone 524, achieving an environmental standard outlet concentration of <5-10 mg / Nm³. At the same time, it can also avoid the impact and wear of dust in the ultra-high temperature flue gas on the waste heat boiler, and prevent dust in the ultra-high temperature flue gas from accumulating, clogging and scaling on the heat exchange surface of the waste heat boiler, thereby improving the stability and safety of the entire ultra-high temperature flue gas purification and filtration and full waste heat recovery system.

[0100] A uniform unloading device 527 is also provided inside the dust collector housing 521. Figure 14 The schematic diagram shows a partially enlarged structure of the uniform unloading device, such as... Figure 14 As shown, the uniform unloading device 527 includes a chute section 5271 fixed with equal gaps within the dust collector housing 521. A bottom support plate 5272 is fixedly installed at a certain distance below the chute section 5271 in the gap area, and a nozzle 5273 is fixedly installed at the midpoint of the bottom support plate 5272. The uniform unloading device 527 ensures that the hot ash in the entire ash hopper is unloaded evenly (avoiding uneven flow), thereby ensuring that the temperature of the hot ash in each layer of the hot ash storage hopper is uniform, which is conducive to achieving high-efficiency heat exchange. The bottom support plate 5272 can be adjusted according to the size of the hot ash's angle of repose (ensuring that the hot ash can reliably stay on the bottom support without automatically flowing down when there is no external force). During production operation, according to the preset control program, the air source of a certain unloading point is pulsedly turned on. Under the boosting action of the boosting air source force, the hot ash is smoothly and evenly unloaded layer by layer from the hot ash storage bin.

[0101] By adopting high-temperature composite phase change heat storage materials to form the bottom plate of the gas inlet tank 523, the separation cavity 5241 of each axial cyclone 524, the gas guide sleeve 5242 of each axial cyclone 524, the top plate of the gas inlet tank 523, and the rigid framework 5244 of the ceramic fiber filter tube 5243, the flue gas filtration and purification device 52 has the function of a heat accumulator, which can store and release the heat energy of the ultra-high-temperature flue gas in a certain ultra-high-temperature range (i.e. 650-950℃) set by the high-temperature composite phase change heat storage device, to solve the contradiction between the supply and demand of heat energy in terms of time and intensity, and basically ensure that the ultra-high-temperature flue gas filtration and purification device 52 operates in a relatively constant ultra-high-temperature range.

[0102] When the ultra-high-temperature flue gas (T≥650-950℃) passes through the device for filtration and purification treatment, the high-temperature composite phase change heat storage material arranged inside can first store part of the heat in the ultra-high-temperature flue gas; when the low-temperature flue gas (T≤450-550℃) passes through the device for filtration and purification treatment, the high-temperature composite phase change heat storage material arranged inside will release the heat accumulated in it when the ultra-high-temperature flue gas passes through, to heat the flue gas. In the entire operation process, the characteristics of the phase change heat storage material working at almost constant temperature near the phase change temperature are fully utilized to reduce the temperature difference between the storage and release of heat, which is more conducive to preventing the thermal shock cracking of the phase change heat storage medium and the ceramic filter material.

[0103] The waste heat recovery device 34 arranged in the reduction system 5 is a waste heat recovery device 34 with finned heat pipes, which includes an upper tank, a waste heat recovery section, a plurality of transition sections, and a lower tank. The upper tank is located above the waste heat recovery section, and the plurality of transition sections are located between the upper tank and the waste heat recovery section. A high-temperature flue gas inlet is arranged above the upper tank, and an access door is arranged above each transition section and the upper tank. A soot blowing device is arranged at the position of the access door to blow and clean the heating surface of the finned heat pipes.

[0104] The shell of the waste heat recovery device 34 is of a membrane water cooling wall structure, and the finned heat pipes are inserted from the outside and can be individually replaced. A special alloy coating layer with heat resistance, wear resistance, and corrosion resistance is sprayed on the surface of the finned heat pipes. The coating layer only needs to have the functions of heat resistance, wear resistance, and corrosion resistance, and thus the specific type of the coating layer is not limited in the present application. The protection of the coating layer can directly reduce the oxidation and wear of the heating surface of the finned heat pipes. The flanges and ceramic fiber bushings can be welded on the heat pipes and fixed on the membrane water cooling wall by fastening screws and gaskets.

[0105] The ash bucket is arranged at the lower part of the waste heat recovery section, and is provided with a cooled flue gas outlet at the bottom of the lower box body on the side corresponding to the inlet of the waste heat recovery section.

[0106] The heat exchanger 36 arranged in the reduction system 5 can ensure maximum absorption of waste heat from the flue gas, and the flue gas is cooled by forced water cooling, and the cooling is performed by using softened water, which can be used as the evaporator water supply of the waste heat recovery device 34 after being heated to a certain degree, so as to realize effective recovery of all waste heat of the converter primary flue gas.

[0107] Figure 15 The overall structure of the converter primary flue gas purification treatment system is schematically shown, and the following will be described in combination with the accompanying drawings. Figure 15 The converter primary flue gas purification treatment system 1 is described in detail. The converter primary flue gas purification treatment system 1 comprises a converter and a vaporization cooling flue 11 communicated with the output end of the converter, and the output end of the vaporization cooling flue 11 is sequentially communicated with a multi-stage flue gas filtration and purification device 52, a waste heat recovery device 34, a heat exchanger 36, a fan 37 and a switching valve 12, and the output end of the switching valve 12 is respectively communicated with a gas cabinet 13 and a diffuser chimney 38. The flue gas filtration and purification device 52, the waste heat recovery device 34, the heat exchanger 36, the fan 37 and the switching valve 12 arranged in the converter primary flue gas purification treatment system 1 are the same as those of the reduction system 5, and the multi-stage flue gas filtration and purification device 52 arranged in the converter primary flue gas purification treatment system 1 is because the capacity of a single set of ultra-high temperature flue gas filtration and purification device 52 is very limited, and multiple sets of devices can be connected in parallel to process the ultra-high temperature flue gas from the converter steelmaking with large flue gas volume.

[0108] The technical scope of the present application is not limited to the above description, and those skilled in the art can make various modifications and changes to the above embodiments without departing from the technical concept of the present application, and these modifications and changes should be within the protection scope of the present application.

Claims

1. A converter primary flue dust resource utilization treatment system, characterized in that, The application relates to a converter primary flue gas purification treatment system (1) and a dust ash treatment system (2) used in cooperation, wherein the dust ash treatment system (2) is connected to the converter primary flue gas purification treatment system (1) to separate and collect iron powder from the dust ash. The dust ash treatment system (2) comprises a first-stage separation and oxidation system (3), a second-stage separation and oxidation system (4) and a reduction system (5) connected in sequence, wherein the first-stage separation and oxidation system (3) and the second-stage separation and oxidation system (4) are used to separate and oxidize magnetic micro-powder in the dust ash, and the magnetic micro-powder is transported to the reduction system (5) to complete the iron powder reduction process and collect the obtained iron powder.

2. The converter primary flue dust resource utilization treatment system according to claim 1, characterized in that, The first-stage separation and oxidation system (3) comprises a first-stage micro-powder magnetic separation device (32), an oxidation roasting furnace (33) and a second-stage micro-powder magnetic separation device (32) connected in sequence, wherein the first-stage micro-powder magnetic separation device (32) and the second-stage micro-powder magnetic separation device (32) are connected to the reduction system (5). The input end of the first-stage micro-powder magnetic separation device (32) is connected to an air flow micro-powder mill (31), and a waste heat recovery device (34) is additionally arranged between the oxidation roasting furnace (33) and the second-stage micro-powder magnetic separation device (32), and the first output end of the second-stage micro-powder magnetic separation device (32) is connected to a dust collector (35). The second output end of the dust collector (35) supplies tailings to the second-stage separation and oxidation system (4), and the first output end of the dust collector (35) is sequentially connected to a heat exchanger (36), a fan (37) and a diffusion chimney (38).

3. The converter primary flue dust resource utilization treatment system according to claim 2, characterized in that, The second-stage separation and oxidation system (4) comprises the air flow micro-powder mill (31), the oxidation roasting furnace (33), the waste heat recovery device (34), the micro-powder magnetic separation device (32), the dust collector (35), the heat exchanger (36), the fan (37) and the diffusion chimney (38) connected in sequence, and the second output end of the micro-powder magnetic separation device (32) is connected to the reduction system (5). The second-stage separation and oxidation system (4) is at least one group, and the second output end of the dust collector (35) is connected to any one of the group or the next group of air flow micro-powder mills (31).

4. The converter primary flue dust resource utilization treatment system according to claim 3, characterized in that, The micro-powder magnetic separation device (32) comprises a smoke dust channel (32a-1) fixedly arranged in the vertical direction, a plurality of separation assemblies fixedly arranged close to the outer edge of the smoke dust channel (32a-1), wherein the separation assemblies are composed of magnetic rotating disc assemblies (32a-2) and discharge grooves (32a-3), the magnetic rotating disc assemblies (32a-2) are fixedly arranged above the discharge grooves (32a-3), cleaning devices are fixedly arranged in the discharge grooves (32a-3), the cleaning devices can be in contact with the surfaces of the magnetic rotating discs, the magnetic rotating discs are a plurality of, the plurality of magnetic rotating discs are coaxially fixed on a rotating drum (32a-4), and the rotating drum (32a-4) is driven by a driving device (32a-5).

5. The converter primary flue dust resource utilization treatment system according to claim 3, characterized in that, The micro-powder magnetic separation device (32) comprises a smoke inlet cavity (32b-1), a shunt cone shell (32b-2) is fixedly arranged in the smoke inlet cavity (32b-1), a dust outlet cavity (32b-3) is fixedly arranged below the smoke inlet cavity (32b-1), a smoke outlet cavity (32b-4) is fixedly arranged below the shunt cone shell (32b-2), and the upper end of the smoke outlet cavity (32b-4) extends into the lower end of the shunt cone shell (32b-2); A magnetic rod frame (32b-5) is arranged on the outer surface of the smoke inlet cavity (32b-1), the magnetic rod frame (32b-5) is matched with the shape of the smoke inlet cavity (32b-1), a plurality of magnetic rods (32b-6) are fixedly arranged on the side of the magnetic rod frame (32b-5) facing the smoke inlet cavity (32b-1), and the magnetic rod frame (32b-5) is rotatably fixedly arranged on the outer surface of the smoke inlet cavity (32b-1).

6. The converter once flue dust resource utilization treatment system according to claim 1, characterized in that, The reduction system (5) comprises a reduction roasting furnace (51), a flue gas filtration and purification device (52), a waste heat recovery device (34), a heat exchanger (36), a fan (37) and a diffusion chimney (38) which are sequentially communicated, the reduction roasting furnace (51) receives the magnetic micro-powder from the primary separation and oxidation system (3) and the secondary separation and oxidation system (4) and completes the reduction process of the magnetic micro-powder.

7. The converter once flue dust resource utilization treatment system according to claim 6, characterized in that, The flue gas filtration and purification device (52) comprises a dust removal shell (521) and a pneumatic conveying device (522) fixedly arranged below the dust removal shell (521) for conveying dust removal ash; An air inlet and an air outlet are formed in the dust removal shell (521), an air inlet box (523) is fixedly arranged in the dust removal shell (521) along the length direction of the air inlet, a plurality of axial cyclone sub-units (524) are fixedly arranged in the air inlet box (523), a blowing assembly (525) is fixedly arranged above the axial cyclone sub-units (524), and an evaporator assembly (526) is fixedly arranged below the air inlet box (523).

8. The converter once flue dust resource utilization treatment system according to claim 7, characterized in that, The axial cyclone sub-unit (524) comprises a separation cavity (5241) fixedly arranged on the bottom plate of the air inlet box (523) and a gas guide assembly fixedly arranged on the top plate of the air inlet box (523); The width of the gas guide assembly is smaller than the width of the side of the separation cavity (5241) close to the gas guide assembly, the gas guide assembly and the separation cavity (5241) are located on the same axis, the lower end of the gas guide assembly is embeddedly fixed with the upper surface of the separation cavity (5241), and the gas guide assembly and the separation cavity (5241) are through. The air guide assembly comprises an air guide sleeve (5242) and a ceramic fiber filter tube (5243) fixed in the air guide sleeve (5242), the air guide sleeve (5242) is a hollow through structure, and a gap for embedding and fixing the ceramic fiber filter tube (5243) is arranged at the upper end of the air guide sleeve (5242); the ceramic fiber filter tube (5243) comprises a rigid framework (5244), a plurality of air holes (5245) are arranged on the rigid framework (5244), and a ceramic fiber membrane (5246) is arranged on the outer edge of the rigid framework (5244); and a baffle is fixedly arranged at the upper end of the ceramic fiber filter tube (5243).

9. The converter once-flue dust resource utilization treatment system according to claim 7, characterized in that, A uniform discharging device (527) is further arranged in the dust removal shell (521), the uniform discharging device (527) comprises a chute section (5271) fixed in the dust removal shell (521) with equal gaps, a bottom supporting plate (5272) is fixedly arranged at a certain distance below the chute section (5271) in the gap region, and a nozzle (5273) is fixedly arranged at the midpoint of the bottom supporting plate (5272).

10. The converter once flue dust dedusting ash resource utilization treatment system according to any one of claims 8-9, characterized in that, The converter primary flue gas purification treatment system (1) comprises a converter and a vaporization cooling flue (11) communicated with the output end of the converter, the output end of the vaporization cooling flue (11) is sequentially connected with a plurality of stages of the flue gas filtration and purification device (52), a waste heat recovery device (34), a heat exchanger (36), a fan (37) and a switching valve (12), and the output end of the switching valve (12) is respectively communicated with a gas tank (13) and a diffusion chimney (38).

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