Converter primary flue gas dedusting ash resource utilization treatment system

Abstract

The invention 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 used in cooperation, and 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. 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 and oxidation reduction, 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 invention relates to the field of energy-saving and environmental protection equipment, and in particular to a converter primary flue gas dust resource utilization processing system. Background Art

[0002] Converter dust is produced during the converter blowing process. Iron-containing dust is produced during the blowing process and is collected by the dust removal system after passing through the flue. Because the steelmaking temperature is high, the temperature of iron-containing dust is high, which can reach 1400°C, and the dust removal system has high requirements. With the development of converter steelmaking production and the improvement of steelmaking technology, the corresponding dust removal technology is also constantly developing and improving. There are two main methods for purifying and recovering steelmaking flue gas. One is wet dust removal, that is, OG dust removal; the other is dry dust removal, that is, LT dust removal. The LT method (dry method) is a dry system for converter flue gas purification and gas recovery developed by a German company and Thyssen Steel Plant. This dust removal method does not use a large amount of turbid water to wash the flue gas, but uses an evaporative cooler + electrostatic precipitator + gas cooler system. In practice, there are also methods that are improved on the basis of the above two dust removal methods, but they can be generally divided into dry and wet methods. However, the LT method can only be called a "semi-dry method" because it uses an evaporative cooler (ie, EC), water spray, and steam spray.

[0003] The output of converter dust is very large. According to relevant statistics, the dust produced by smelting 1 ton of steel is 15-20 kg. If the annual crude steel output is 1 billion tons, and 18 kg of dust is produced per ton of steel, the annual dust produced is 18 million tons. With the continuous expansion of steel production capacity, the output of converter dust will increase year by year.

[0004] The iron content in converter dust is high, TFe>50%, which is a high-quality iron-containing resource. If it is not used, it will not only cause a waste of resources, but also occupy a large amount of land for its stacking, and may also cause environmental pollution. From the perspective of metallurgy, converter dust ash has fine particle size, high iron content, and high CaO content, which are its significant characteristics. Therefore, the dust collected by emission reduction must be recycled by all means to turn waste into treasure. It can not only make rational use of resources but also reduce environmental pollution.

[0005] At present, the main treatment technologies for primary converter dust removal include returning sintering and pelletizing as raw materials for ironmaking, pressing into blocks and returning to the converter as coolant, and other internal circulation schemes in steel mills. Elements such as K, Na, and Zn in dust removal ash will have an adverse effect on blast furnace smelting, and elements such as P and S will have an adverse effect on steel quality. The internal recycling of dust removal ash in steel mills is not only not conducive to steel production, but also has low added value.

[0006] There is increasing concern about the development and utilization of converter primary dust as secondary resources and the effective separation of the Fe contained therein. It is urgent to develop a new process technology for the resource utilization of converter primary dust. Summary of the invention

[0007] The technical problem to be solved by the present invention is to overcome the defects of the prior art. The present invention proposes a resource utilization and processing system for dust removal ash of primary flue gas of a converter, studies the composition of the dust removal ash, uses an oxidation-reduction method to sort the Fe contained in the dust removal ash, and realizes pure dry purification treatment of the primary flue gas of the converter.

[0008] In order to solve the above technical problems, the technical solution adopted by the present invention is: a converter primary flue gas dust ash resource utilization treatment system, comprising a converter primary flue gas purification treatment system and a dust ash treatment system used in conjunction, the dust ash treatment system receives the dust ash from the converter primary flue gas purification treatment system, and separates and collects iron powder from the dust ash;

[0009] The dust ash treatment system includes a primary sorting oxidation system, a secondary sorting oxidation system and a reduction system which are connected in sequence. The primary sorting oxidation system and the secondary sorting oxidation system collect the magnetic micropowder in the dust ash after sorting and oxidation, and transport the magnetic micropowder to the reduction system to complete the iron powder reduction process and collect the obtained iron powder.

[0010] Furthermore, the primary separation oxidation system comprises a first-stage micro-powder magnetic separation device, an oxidation roasting furnace and a second-stage micro-powder magnetic separation device which are connected in sequence, and the second output ends of the first-stage micro-powder magnetic separation device and the second-stage micro-powder magnetic separation device are both connected to the reduction system;

[0011] The input end of the first-stage micro-powder magnetic separation device is connected to the airflow micro-powder mill, a waste heat recovery device is further provided between the oxidation roasting furnace and the second-stage micro-powder magnetic separation device, and the first output end of the second micro-powder magnetic separation device is connected to the dust collector;

[0012] The second output end of the dust collector supplies tailings to the secondary sorting oxidation system, and the first output end of the dust collector is sequentially connected to a heat exchanger, a fan and a dispersing chimney.

[0013] Furthermore, the secondary separation oxidation system comprises an airflow micro-powder mill, an oxidation roasting furnace, a waste heat recovery device, a micro-powder magnetic separation device, a dust collector, a heat exchanger, a fan and a venting chimney which are connected in sequence, and the second output end of the micro-powder magnetic separation device is connected to the reduction system;

[0014] The secondary sorting oxidation system is at least one group, and the second output end of the dust collector is connected to any one of the airflow micro-powder mills in this group or the next group.

[0015] Furthermore, the micro-powder magnetic separation device includes a smoke and dust channel fixedly arranged vertically, and a plurality of separation components are fixedly arranged close to the outer edge of the smoke and dust channel. The separation component is composed of a magnetic rotating disk assembly and a discharge chute. The magnetic rotating disk assembly is fixedly arranged above the discharge chute. A cleaning device is fixedly arranged in the discharge chute, and the cleaning device can contact the surface of the magnetic rotating disk. There are multiple magnetic rotating disks, and the multiple magnetic rotating disks are coaxially fixed on the rotating drum, and the rotating drum is driven by a driving device.

[0016] Furthermore, the micro-powder magnetic separation device comprises a smoke inlet cavity, a flow dividing cone shell is fixedly arranged in the smoke inlet cavity, a dust outlet cavity is fixedly arranged below the smoke inlet cavity, a smoke outlet cavity is fixedly arranged below the flow dividing cone shell, and the upper end of the smoke outlet cavity extends into the lower end of the flow dividing cone shell;

[0017] A magnetic rod rack is arranged on the outer surface of the smoke inlet cavity, the magnetic rod rack matches the shape of the smoke inlet cavity and a plurality of magnetic rods are fixedly arranged on the side of the magnetic rod rack facing the smoke inlet cavity, and the magnetic rod rack is rotatably fixed on the outer surface of the smoke inlet cavity.

[0018] Furthermore, the reduction system includes a reduction roasting furnace, a flue gas filtering and purification device, a waste heat recovery device, a heat exchanger, a fan and a discharge chimney which are connected in sequence. The reduction roasting furnace receives the magnetic micropowder from the primary sorting oxidation system and the secondary sorting oxidation system and completes the reduction process of the magnetic micropowder.

[0019] Furthermore, the fume filtration and purification device comprises a dust removal housing and a pneumatic conveying device fixedly arranged below the dust removal housing for conveying dust removal ash;

[0020] An air inlet and an air outlet are provided on the dust removal shell, an air inlet box is fixedly arranged along the length direction of the air inlet and inside the dust removal shell, a plurality of axial cyclones are fixedly arranged in the air inlet box, a spray assembly is fixedly arranged above the axial cyclones; an evaporator assembly is fixedly arranged below the air inlet box.

[0021] Further, the axial cyclone comprises a separation cavity fixedly arranged on the bottom plate of the air intake box and an air guide assembly fixedly arranged on the top plate of the air intake box;

[0022] The width of the air guide component is smaller than the width of the separation cavity on one side close to the air guide component, the air guide component and the separation cavity are located on the same axis, the lower end of the air guide component is embedded and fixed with the upper surface of the separation cavity, and the air guide component and the separation cavity are connected;

[0023] The air guide assembly includes an air guide sleeve and a ceramic fiber filter tube fixed in the air guide sleeve. The air guide sleeve is a hollow through structure, and a notch is provided at the upper end of the air guide sleeve for the ceramic fiber filter tube to be embedded and fixed; the ceramic fiber filter tube includes a rigid frame, and a plurality of air holes are opened on the rigid frame. The outer edge of the rigid frame is covered with a ceramic fiber membrane, and a baffle is fixedly provided at the upper end of the ceramic fiber filter tube.

[0024] Furthermore, a uniform unloading device is also provided in the dust removal shell, and the uniform unloading device includes a chute section fixed with equal gaps in the dust removal shell, a bottom support plate is fixedly provided in the gap area at a certain distance below the chute section, and a nozzle is fixedly provided at the midpoint of the bottom support plate.

[0025] Furthermore, the converter primary flue gas purification treatment system includes a converter and a vaporization cooling flue connected to the output end of the converter, the output end of the vaporization cooling flue is sequentially connected to a multi-stage flue gas filtration and purification device, a waste heat recovery device, a heat exchanger, a fan and a switching valve, and the output end of the switching valve is respectively connected to a gas tank and a venting chimney.

[0026] Compared with the prior art, the beneficial effects of the present invention include:

[0027] 1) The dust ash is collected by the converter primary flue gas purification system and then handed over to the dust ash treatment system. After sorting, oxidation and reduction, the Fe and its oxides contained in the dust ash are converted into Fe powder, and the Fe contained in the dust ash is effectively sorted to realize the resource utilization of the converter primary flue gas dust ash; in the process of treating the dust ash, the magnetic Fe and Fe3O4 in the dust ash are first separated, and then the FeO, FeO2 and Fe2O3 in the dust ash are converted into Fe and Fe3O4 through an oxidation process, and Fe is used as a reducing agent in the reduction process. No additional additives are added in the process, and there is no impact on the dust ash itself, and the effective recovery of waste heat is simultaneously realized;

[0028] 2) By applying the flue gas filtration and purification device in the primary flue gas purification system and the reduction system of the converter, the ceramic fiber filter tube set in the central air guide sleeve of each axial cyclone can realize the ultra-clean filtration of the ultra-high temperature flue gas, reaching the environmental protection standard outlet concentration of <5-10mg / Nm 3At 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 avoid the dust in the ultra-high temperature flue gas from gathering, clogging and scaling on the heat exchange surface of the waste heat boiler, thereby improving the stability and safety of the operation of the entire ultra-high temperature flue gas purification and filtration and full waste heat recovery system, and by using high-temperature composite phase change heat storage materials to respectively form the bottom plate of the air intake box, the separation cavity of each axial cyclone, the air guide sleeve of each axial cyclone, the top plate of the air intake box and the rigid skeleton of the ceramic fiber filter tube, the flue gas filtration and purification device 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 section set by the high-temperature composite phase change heat storage device for the discontinuous characteristics of electric furnace steelmaking or converter steelmaking, so as to solve the contradiction between the mismatch between heat energy supply and demand in time and intensity, and basically ensure that the ultra-high temperature flue gas filtration and purification device is operated in a relatively constant ultra-high temperature range;

[0029] 3) Adopt pure dry dust removal technology to achieve "0" consumption of water and steam in the process of converter primary flue gas purification, full waste heat recovery of converter and converter primary flue gas, clean dry gas recovery (increases the calorific value of gas), ultra-low flue gas emission (dust content of flue gas ≤5-10mg / Nm 3 ), avoids secondary pollution, and also creates favorable conditions for the secondary resource utilization of the converter primary dust. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] The disclosure of the present invention is described with reference to the accompanying drawings. It should be understood that the drawings are for illustrative purposes only and are not intended to limit the scope of protection of the present invention. In the accompanying drawings, the same reference numerals are used to refer to the same components. Among them:

[0031] Figure 1 The overall structure of the converter primary flue gas dust ash resource utilization treatment system is schematically shown;

[0032] Figure 2 The overall structure of the dust removal ash handling system is schematically shown;

[0033] Figure 3 The overall structure of the primary sorting oxidation system is schematically shown;

[0034] Figure 4 The overall structure of the two-stage separation oxidation system is schematically shown;

[0035] Figure 5 The cross-sectional structure of a multi-wheel disc-type micro-powder magnetic separation device is schematically shown;

[0036] Figure 6 The cross-sectional structure of the magnetic rotating disk assembly is schematically shown;

[0037] Figure 7 The cross-sectional structure of a magnetic bar type micro powder magnetic separation device is schematically shown;

[0038] Figure 8 The overall structure of the reduction system is shown schematically;

[0039] Fig. 9 The cross-sectional structure of the flue gas filtering and purification device is schematically shown;

[0040] Fig.10 The cross-sectional structure of the axial cyclone is schematically shown;

[0041] Fig.11 The cross-sectional structure of the gas guide assembly is schematically shown;

[0042] Fig.12 The cross-sectional structure of the gas guide tube is schematically shown;

[0043] Fig.13 The cross-sectional structure of the ceramic fiber filter tube is schematically shown;

[0044] Fig.14 The schematic diagram shows a partial enlarged structure of the uniform unloading device;

[0045] Fig.15 The overall structure of the converter primary flue gas purification system is schematically shown.

[0046] Numbers in the figure:

[0047] 1. Converter primary flue gas purification system, 2. Dust removal ash treatment system, 3. Primary sorting oxidation system, 4. Secondary sorting oxidation system, 5. Reduction system;

[0048] 11. Vaporization cooling flue, 12. Switching valve, 13. Gas tank;

[0049] 31. Air flow 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. Dispersion chimney;

[0050] 51. Reduction roasting furnace, 52. Flue gas filtering and purification device;

[0051] 521. dust removal housing, 522. pneumatic conveying device, 523. air inlet box, 524. axial cyclone, 525. spray assembly, 526. evaporator assembly, 527. uniform unloading device;

[0052] 5241. separation chamber, 5242. air guide sleeve, 5243. ceramic fiber filter tube, 5244. rigid frame, 5245. vent hole, 5246. ceramic fiber membrane;

[0053] 5251, pulse jet pipe, 5252, air storage bag, 5253, pulse jet solenoid valve;

[0054] 5271, slide pipe section, 5272 bottom support plate, 5273 nozzle;

[0055] 32a-1, smoke and dust channel, 32a-2, magnetic rotating disk assembly, 32a-3, discharge chute, 32a-4, rotating drum, 32a-5, driving device;

[0056] 32b-1, smoke inlet cavity, 32b-2, diversion cone shell, 32b-3, dust outlet cavity, 32b-4, smoke outlet cavity, 32b-5, magnetic rod rack, 32b-6, magnetic rod. DETAILED DESCRIPTION

[0057] It is easy to understand that according to the technical solution of the present invention, without changing the essential spirit of the present invention, a person skilled in the art can propose a variety of interchangeable structural modes and implementation modes. Therefore, the following specific implementation modes and drawings are only exemplary descriptions of the technical solution of the present invention, and should not be regarded as the whole of the present invention or as a limitation or restriction to the technical solution of the present invention.

[0058] Figure 1 The overall structure of the converter primary flue gas dust ash resource utilization treatment system is schematically shown. A converter primary flue gas dust ash resource utilization treatment system is shown. Figure 1 As shown, it includes a converter primary flue gas purification system 1 and a dust ash treatment system 2 used in conjunction with each other, wherein the converter primary flue gas purification system 1 directly receives the flue gas output from the converter steelmaking process, and adsorbs and collects the impurities in the flue gas to form dust ash, and the treated flue gas can be selectively discharged directly or stored in a gas tank 13 after the waste heat is recovered; the aforementioned dust ash enters the dust ash treatment system 2, because the converter primary dust ash contains Fe, FeO, FeO2, Fe2O3 and Fe3O4 particles and the particle sizes of the particles are different, the Fe particles cannot be directly obtained, and therefore, oxidation reaction and reduction reaction are required to prepare the aforementioned mixed particles to convert the FeO, FeO2, Fe2O3, and Fe3O4 particles into Fe particles and then recover the Fe powder.

[0059] Figure 2 The overall structure of the dust removal and ash handling system is shown schematically. Figure 2As shown, the dust ash treatment system 2 comprises a primary sorting oxidation system 3, a secondary sorting oxidation system 4 and a reduction system 5 which are connected in sequence. The primary sorting oxidation system 3 and the secondary sorting oxidation system 4 preliminarily sort the magnetic Fe and Fe3O4 particles (i.e., magnetic micropowder) contained in the dust ash, and then apply an oxidation reaction. At 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 micropowder particles contained therein are oxidized into Fe3O4 (with magnetism), creating conditions for sorting FeO, FeO2, and Fe2O3 iron oxide micropowder particles from the micropowder, and then a secondary sorting is performed to sort out most of the Fe-containing particles. After that, the secondary oxidation sorting system 4 performs secondary oxidation sorting to basically convert the Fe contained in the dust ash into Fe and Fe3O4 particles. Then, the dust ash enters the reduction system 5. Under the furnace temperature condition of 570℃<T10<1000℃, CO+H2 gas is introduced to reduce the magnetic micropowder particles such as Fe and Fe3O4 into reduced iron powder and collect them, thereby completing the recovery process of the Fe powder in the dust ash and realizing the resource utilization of the dust ash.

[0060] Figure 3 The overall structure of the primary separation oxidation system is shown schematically. Figure 3 As shown, the aforementioned primary separation oxidation system 3 includes a first-stage micro-powder magnetic separation device 32, an oxidation roasting furnace 33 and a second-stage micro-powder magnetic separation device 32 which are connected in sequence, and the second output ends of the first-stage micro-powder magnetic separation device 32 and the second-stage micro-powder magnetic separation device 32 are both connected to the reduction system 5. The input end of the first-stage micro-powder magnetic separation device 32 is connected to the airflow micro-powder mill 31, and a waste heat recovery device 34 is additionally provided between the oxidation roasting furnace 33 and the second-stage micro-powder magnetic separation device 32 for recovering the waste heat of the dust removal ash. The first output end of the second 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 secondary separation oxidation system 4, and the first output end thereof is connected to a heat exchanger 36, a fan 37 and a dissipation chimney 38 in sequence.

[0061] The specific process of primary sorting is as follows:

[0062] (1) Air flow crushing / sorting

[0063] First, the hot ash in the ash hopper of the ultra-high temperature flue gas filtration and purification device 52 of the converter primary pure dry purification system is sent to the air flow micro powder mill 31 for crushing / sorting through high-pressure nitrogen. The air flow micro powder mill 31 peels off the surface of Fe, FeO, FeO2, Fe2O3, and Fe3O4 particles in the converter primary dust removal ash, so as to remove impurities on the surface of Fe, FeO, FeO2, Fe2O3, and Fe3O4 particles, sort out micro powder with a particle size of D50≤10μm, and increase the surface area and activity of micro powder.

[0064] (2) First-stage powder magnetic separation

[0065] A first-stage powder magnetic separation device is installed on the conveying air duct that sends the fine powder material with a particle size of D50≤10μm crushed / sorted by air flow to the next process, and the magnetic fine powder particles such as Fe and Fe3O4 in the fine powder are separated and sent to the reduction process to make reduced iron powder.

[0066] The mechanism of the micro powder magnetic separation device installed on the flue:

[0067] Fe and Fe3O4 powder particles can be separated into monomers when they are ≤30-50μm. At this particle size, traditional magnetic separation equipment cannot separate Fe and Fe3O4 powder particles from other mineral powder particles. This is because at this particle size, under the action of strong magnetic field, Fe and Fe3O4 powder particles and other mineral powder particles in the powder undergo magnetic agglomeration and electrostatic adsorption, making it impossible to achieve effective separation. The primary dust removal of converter ash powder is a fully dry process, which requires that the monomers of Fe and Fe3O4 powder particles and other mineral powder particles in the powder be dispersed in gas (nitrogen or air), so that it is possible to effectively separate Fe and Fe3O4 powder particles under the action of magnetic field force.

[0068] (3) Oxidation

[0069] A set of oxidation roasting furnace 33 is provided. The powder material after the first-stage powder magnetic separation is sent into the powder roasting furnace, and CO+O2 is introduced at a process temperature of T<570℃ to oxidize the powder, so that the iron oxide powder particles such as FeO, FeO2, and Fe2O3 contained therein are oxidized into Fe3O4 (with magnetic properties), creating conditions for separating the iron oxide powder particles such as FeO, FeO2, and Fe2O3 from the powder.

[0070] The oxidation reaction of this process is as follows:

[0071] T<570℃

[0072] Fe2O3+3CO— 加热 —→Fe3O4+3CO2

[0073] Fe2O3+4FeO— 加热 —→Fe+Fe3O4

[0074] (4) Cooling

[0075] A waste heat recovery device 34 with finned heat pipes (also serving as waste heat recovery device 34) is provided after the oxidation roasting furnace 33. In order to ensure that the second-stage fine powder magnetic separation can separate Fe3O4 from the fine powder in the roasting furnace, the smoke must be cooled to a certain extent to ensure that the Fe3O4 fine powder particles have magnetic properties.

[0076] (5) Second stage powder magnetic separation

[0077] A second-stage micro-powder magnetic separation device is arranged on the conveying air duct between the waste heat recovery device 34 with finned heat pipes and the high-temperature resistant ultra-low emission pulse jet bag / flexible metal membrane cartridge dust collector 35 to separate the magnetic micro-powder particles such as Fe and Fe3O4 in the micro-powder and send them to the reduction process to be made into reduced iron powder.

[0078] (6) Exhaust gas purification treatment

[0079] A set of 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 separation device to filter and purify the exhaust smoke after the second-stage micro powder magnetic separation to ensure that the exhaust dust content is ≤5-10mg / Nm 3 The collected tail powder is sent to the secondary sorting process for further sorting.

[0080] Figure 4 The overall structure of the two-stage separation oxidation system is shown schematically. Figure 4 As shown, the aforementioned secondary sorting oxidation system 4 includes 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 which are connected in sequence, and 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 need to perform a magnetic separation process on 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, and the rest of the structure is completely consistent with the primary sorting oxidation system 3, and in the secondary sorting process, it only lacks the first-stage micro-powder magnetic sorting process as in the primary sorting process, and the rest of the process is completely consistent with the primary sorting process.

[0081] It is worth noting that the second output end of the dust collector 35 of 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 so as to completely convert the FeO, FeO2 and Fe2O3 in the dust ash into magnetic micro-powder. In another embodiment, multiple groups of secondary sorting oxidation systems 4 can be set up, and the second output end of the previous group of secondary sorting oxidation systems 4 can be connected to the airflow micro-powder mill 31 of the next group of secondary sorting systems. However, this embodiment requires the setting of multiple groups of secondary sorting oxidation systems 4, which has too high a space requirement.

[0082] The fine powder magnetic separation device 32 involved in the aforementioned primary separation oxidation system 3 and the secondary separation oxidation system 4 can be a multi-wheel disc type or a magnetic rod type. The aforementioned fine powder magnetic separation device 32 is specifically described below.

[0083] Figure 5 The schematic diagram shows the cross-sectional structure of the multi-wheel disc type micro powder magnetic separation device, such as Figure 5 As shown, a powder magnetic separator (multi-wheel disc type) includes a smoke and dust channel 32a-1 fixedly arranged vertically, and a plurality of sorting components fixedly arranged close to the outer edge of the smoke and dust channel 32a-1, the sorting component consists of a magnetic rotating disk component 32a-2 and a discharge trough 32a-3, the magnetic rotating disk component 32a-2 is fixedly arranged above the discharge trough 32a-3, and a cleaning device is fixedly arranged in the discharge trough 32a-3, the cleaning device can contact with the surface of the magnetic rotating disk, wherein only a part of the area of ​​the magnetic rotating disk is magnetic, such as half of the area above the magnetic rotating disk is magnetic, then only the magnetic area of ​​the magnetic rotating disk can absorb magnetic powder, and when the magnetic area rotates to the cleaning device area, the cleaning device contacts the surface of the magnetic area, thereby scraping off the magnetic powder adsorbed on the magnetic area, and the scraped magnetic powder will fall into the discharge trough 32a-3, thereby completing the collection process of the magnetic powder.

[0084] Figure 6 The cross-sectional structure of the magnetic rotating disk assembly is schematically shown, as Figure 6 As shown, the aforementioned magnetic rotating disk may be multiple, and multiple magnetic rotating disks are coaxially fixed on the rotating drum 32a-4 to form a magnetic rotating disk assembly. The rotating drum 32a-4 is driven to rotate by the driving device 32a-5, thereby driving the magnetic rotating disk located thereon to rotate coaxially.

[0085] In order to make the magnetic rotating disk adsorb the magnetic micropowder in the smoke more completely, a diversion device is fixedly installed in the smoke channel 32a-1, which is used to divert the smoke channel 32a-1 into multiple smoke channel 32a-1 branches with smaller diameters. Multiple groups of magnetic rotating disks are provided on each smoke channel 32a-1 branch to complete the adsorption of magnetic micropowder. The content of magnetic micropowder in the smoke after diversion can be significantly reduced, and multiple groups of magnetic rotating disks are provided for adsorption, which can maximize the adsorption effect of the magnetic micropowder in the smoke passing through.

[0086] Figure 7 The cross-sectional structure of the magnetic rod type micro powder magnetic separation device is schematically shown. Figure 7 As shown, a micro powder magnetic separator (magnetic rod type) includes a smoke inlet cavity 32b-1, in which a diverter cone shell 32b-2 is fixedly arranged. After the smoke enters the smoke inlet cavity 32b-1 from the smoke inlet of the smoke inlet cavity 32b-1, the diverter process is completed under the action of the tip of the diverter cone shell 32b-2. Since the diverter cone shell 32b-2 is fixedly arranged in the middle position of the smoke inlet cavity 32b-1, the diverted smoke will flow closely against the side wall of the smoke inlet cavity 32b-1; a dust outlet cavity 32b-3 is fixedly arranged below the smoke inlet cavity 32b-1, and a dust outlet cavity 32b-3 is fixedly arranged below the diverter cone shell 32b-2. A smoke outlet cavity 32b-4 is fixedly provided, and the smoke outlet cavity 32b-4 is located in the middle position of the smoke inlet cavity 32b-1, and the dust outlet cavity 32b-3 is arranged around the aforementioned smoke outlet cavity 32b-4, which is used to cooperate with the diversion flow mode of the smoke. The upper section of the aforementioned smoke outlet cavity 32b-4 extends into the lower end of the diversion cone shell 32b-2. Such an arrangement can make the smoke entering the smoke inlet cavity 32b-1 first flow along the edge of the smoke inlet cavity 32b-1 under the action of the diversion cone shell 32b-2, and then enter the lower end of the diversion cone shell 32b-2 to complete the output from the smoke outlet cavity 32b-4.

[0087] Based on the aforementioned outer surface of the smoke inlet cavity 32b-1, a magnetic rod rack 32b-5 is provided, the magnetic rod rack 32b-5 matches the shape of the smoke inlet cavity 32b-1, and a plurality of magnetic rods 32b-6 are fixedly provided on the side of the magnetic rod rack 32b-5 facing the smoke inlet cavity 32b-1. For example, if the smoke inlet cavity 32b-1 is a cylindrical structure, the magnetic rod rack 32b-5 is an annular structure matching the outer edge of the cylindrical structure, so that it can be tightly attached to the outer edge surface of the smoke inlet cavity 32b-1, and the aforementioned magnetic rods 32b-6 are in close contact with the outer edge surface of the smoke inlet cavity 32b-1, and the magnetic rod rack 32b-5 can be rotatably fixedly provided on the smoke inlet cavity 32b-1. 2b-1, specifically, a fixed point is provided on the outer surface of the smoke inlet chamber 32b-1, and the magnetic rod frame 32b-5 is fixed to the fixed point with a column, so that the magnetic rod frame 32b-5 can rotate around the fixed point and a telescopic component such as a cylinder is vertically arranged above the smoke inlet of the smoke inlet chamber 32b-1. The side of the magnetic rod frame 32b-5 away from the smoke inlet chamber 32b-1 is an inverted triangle, and a corner away from the smoke inlet chamber 32b-1 is fixed to the aforementioned telescopic component to drive this corner to move up and down, so that the magnetic rod frame 32b-5 can rotate along the aforementioned fixed point.

[0088] When the aforementioned magnetic rod rack 32b-5 is in close contact with the side of the smoke inlet chamber 32b-1, the magnetic force of the magnetic rod 32b-6 located thereon can act on the smoke flowing through the smoke inlet chamber 32b-1, and adsorb the magnetic micropowder therein to the side wall of the smoke inlet chamber 32b-1. After all the smoke is discharged, the magnetic rod rack 32b-5 is moved away from the aforementioned smoke inlet chamber 32b-1, and the magnetic micropowder adsorbed on the inner wall of the smoke inlet chamber 32b-1 can fall into the dust outlet chamber 32b-3 under the action of gravity, thereby completing the collection of the magnetic micropowder.

[0089] The micro-powder magnetic separation device 32 of the first-stage micro-powder magnetic separation device 32 and the micro-powder magnetic separation device 32 of the second-stage micro-powder magnetic separation device 32 in the aforementioned first-stage sorting oxidation system 3 and the micro-powder magnetic separation device 32 in the secondary sorting oxidation system 4 can be selected from any one of the aforementioned multi-wheel disc type micro-powder magnetic separation device 32 or the magnetic rod rack 32b-5 type micro-powder magnetic separation device 32.

[0090] Figure 8 The overall structure of the reduction system is shown schematically. Figure 8The reduction system 5 is described in detail. The reduction system 5 includes a reduction roasting furnace 51, a flue gas filtering and purification device 52, a waste heat recovery device 34, a heat exchanger 36, a fan 37 and a dissipation chimney 38 which are connected in sequence. The reduction roasting furnace 51 receives the magnetic micropowder from the primary separation oxidation system 3 and the secondary separation oxidation system 4 and completes the reduction process of the magnetic micropowder. The specific process of preparing the reduced Fe powder is as follows:

[0091] The magnetic powder particles such as Fe and Fe3O4 separated by magnetic separation in the above-mentioned primary / secondary separation process are sent to the reduction roasting furnace 51. Under the furnace temperature condition of 570℃<T10<1000℃, CO+H2 gas is introduced to reduce the magnetic powder particles such as Fe and Fe3O4 into reduced iron powder. The reduced iron powder is collected by the ultra-high temperature flue gas filtration and purification device 52, cooled, and then packaged and transported away.

[0092] The reduction reaction of this step is as follows:

[0093] At 570℃<T<1000℃

[0094] ① Reduction with CO:

[0095] Fe3O4+4CO— 加热 —→3Fe+4CO2

[0096] ② Reduction with H2:

[0097] Fe3O4+4H2— 加热 —→3Fe+4H2O

[0098] Fig. 9 The cross-sectional structure of the flue gas filtration and purification device is schematically shown. Fig. 9As shown, the flue gas filtering and purification device 52 located in the aforementioned reduction system 5 includes a dust removal shell 521 and a pneumatic conveying device 522 fixedly arranged below the dust removal shell 521 for conveying dust ash; an air inlet and an air outlet are opened on the dust removal shell 521, and an air intake 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 intake 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 intake box 523. The aforementioned blowing assembly 525 includes a pulse blowing pipe 5251 and an air storage bag 5252 for supplying air to the pulse blowing pipe 5251. A pulse blowing solenoid valve 5253 is fixedly arranged between the pulse blowing pipe 5251 and the air storage bag 5252 for regulating the blowing process. The aforementioned air storage bag 5252 is connected to the nitrogen source of the pneumatic conveying device 522, that is, the nitrogen stored in the air storage bag 5252 is the same as that of the pneumatic conveying device 522. 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.

[0099] Fig.10 The schematic diagram shows the cross-sectional structure of the axial cyclone. Fig.10 As shown, the aforementioned axial cyclone 524 includes a separation chamber 5241 fixedly arranged on the bottom plate of the air inlet box 523 and an air guide assembly fixedly arranged on the top plate of the air inlet box 523; wherein the width of the air guide assembly is smaller than the width of the separation chamber 5241 close to the side of the air guide assembly, the air guide assembly and the separation chamber 5241 are located on the same axis, a fixed port is fixedly arranged on the upper end of the separation chamber 5241, and a vortex flow guide plate is fixedly arranged between the fixed port and the inner surface of the separation chamber 5241, the lower end of the air guide assembly is embedded and fixed with the upper surface of the separation chamber 5241, and the air guide assembly and the separation chamber 5241 are connected, specifically, the outer diameter width of the aforementioned fixed port is not greater than the inner diameter width of the lower end of the air guide assembly, so that the lower end of the air guide assembly can be embedded and fixed with the aforementioned fixed port, and the air guide assembly and the separation chamber 5241 are connected through the fixed port.

[0100] Fig.11 The cross-sectional structure of the gas guide component is schematically shown. Fig.11 As shown, the aforementioned air guide assembly includes an air guide sleeve 5242 and a ceramic fiber filter tube 5243 fixed in the air guide sleeve 5242. Fig.12 The cross-sectional structure of the gas guide tube is schematically shown. Fig.12As shown, the air guide sleeve 5242 is a hollow through structure, and a notch is provided at the top of the air guide sleeve 5242 for the ceramic fiber filter tube 5243 to be embedded and fixed, and a convex ring is provided on the outer edge surface. The air guide sleeve 5242 can be inserted from the top plate of the air intake box 523, and the upper end of the air guide sleeve 5242 can be limited on the top plate of the air intake box 523 by the convex ring provided on its outer edge surface.

[0101] Fig.13 The cross-sectional structure of the ceramic fiber filter tube is schematically shown. Fig.13 As shown, the aforementioned ceramic fiber filter tube 5243 includes a rigid frame 5244, a plurality of ventilation holes 5245 are opened on the rigid frame 5244 along the width direction of the rigid frame 5244, and a ceramic fiber membrane 5246 is coated on the outer edge of the rigid frame 5244, and a baffle is fixedly arranged on 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 arranged at the top of the air guide sleeve 5242, and the upper end of the ceramic fiber filter tube 5243 is limited at the upper end of the air guide sleeve 5242 by the baffle, thereby fixing the ceramic fiber filter tube 5243 in the aforementioned air guide sleeve 5242.

[0102] The ceramic fiber filter tube 5243 disposed in the central air guide sleeve 5242 of each cyclone 524 realizes ultra-clean filtration of the ultra-high temperature flue gas, reaching the environmental protection standard outlet concentration of <5-10mg / Nm 3 At the same time, it can also avoid the impact and wear of dust in ultra-high temperature flue gas on the waste heat boiler, and avoid the dust in ultra-high temperature flue gas from gathering, 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.

[0103] A uniform unloading device 527 is also provided in the dust removal housing 521. Fig.14 The schematic diagram shows the partial enlarged structure of the uniform unloading device, such as Fig.14As shown, the uniform unloading device 527 includes a chute section 5271 fixed in the dust removal housing 521 with equal gaps, a bottom support plate 5272 is fixedly arranged at a certain distance below the chute section 5271 in the gap area, and a nozzle 5273 is fixedly arranged at the midpoint of the bottom support plate 5272. The setting of the uniform unloading device 527 can ensure the overall balanced unloading of the hot ash in the entire ash hopper (avoiding bias flow), thereby ensuring that the temperature of each layer section of the hot ash in the hot ash storage hopper is balanced, 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 resting angle (to ensure that the hot ash can reliably stagnate on the bottom support material and will not automatically flow down when there is no external force). During production operation, according to the pre-set control program, the gas source of a certain unloading point is pulsed and opened respectively, and the hot ash is smoothly and evenly discharged layer by layer from the hot ash storage bin under the boosting effect of the boosting gas source force.

[0104] By adopting high-temperature composite phase-change heat storage materials to respectively form the bottom plate of the air intake box 523, the separation cavity 5241 of each axial cyclone 524, the air guide sleeve 5242 of each axial cyclone 524, the top plate of the air intake box 523 and the rigid frame 5244 of the ceramic fiber filter tube 5243, the flue gas filtering and purification device 52 has the function of a heat storage device. It can store and release the heat energy of ultra-high temperature flue gas in a set ultra-high temperature section (i.e., 650-950°C) according to the discontinuous characteristics of production such as electric furnace steelmaking or converter steelmaking, so as to solve the contradiction between the mismatch between heat energy supply and demand in time and intensity, and basically ensure that the ultra-high temperature flue gas filtering and purification device 52 is operated in a relatively constant ultra-high temperature range.

[0105] When ultra-high temperature flue gas (T≥650~950℃) passes through the device for filtration and purification, the high temperature composite phase change thermal storage material installed inside it will first store part of the heat in the ultra-high temperature flue gas through its huge latent heat capacity; and when low temperature flue gas (T≤450~550℃) passes through the device for filtration and purification, the high temperature composite phase change thermal storage material installed inside it will release the heat accumulated in it when the ultra-high temperature flue gas passes through it, and heat the flue gas. During the entire operation process, the characteristics of the phase change thermal storage material working at an almost constant temperature near the phase change temperature are fully utilized to reduce the temperature difference between heat release and heat release, which is more conducive to preventing the thermal shock cracking problem of the phase change thermal storage medium and the ceramic filter material.

[0106] The waste heat recovery device 34 arranged in the reduction system 5 is a waste heat recovery device 34 with finned heat pipes, and the waste heat recovery device 34 includes an upper box body, a waste heat recovery section, multiple transition sections and a lower box body, wherein the upper box body is located above the waste heat recovery section, and the multiple transition sections are located between the upper box body and the waste heat recovery section. A high-temperature flue gas inlet is arranged on the upper box body, and maintenance doors are respectively arranged on the upper box body and each transition section, and a soot blowing device is arranged at the position of the maintenance door for spraying and cleaning the heating surface of the finned heat pipe.

[0107] The shell of the waste heat recovery device 34 adopts a membrane water-cooled wall structure as a whole, and is provided with a finned heat pipe with a replaceable heating surface inserted from the outside, and a layer of heat-resistant, wear-resistant, and corrosion-resistant special alloy coating is sprayed on the surface of the finned heat pipe. Since the coating only needs to enable the finned heat pipe to have the corresponding heat-resistant, wear-resistant, and corrosion-resistant functions, the present invention does not specifically limit it here. The protection of the coating can directly reduce the degree of oxidation and wear of the heating surface of the finned heat pipe, which can be fixed on the membrane water-cooled wall by welding a flange and a ceramic fiber bushing on the heat pipe and fastening screws and washers.

[0108] It also includes an ash hopper, which is located at the lower part of the waste heat recovery section. A cooled flue gas outlet is arranged at the bottom of the lower box body on one side of the ash hopper corresponding to the inlet of the waste heat recovery section. A flame retardant / explosion-proof compressed nitrogen injection device is arranged in each waste heat recovery section, and a fluidized compressed nitrogen injection device is arranged at the bottom of the ash hopper.

[0109] The heat exchanger 36 arranged in the reduction system 5 can ensure that the waste heat is absorbed from the flue gas to the maximum extent. The flue gas is cooled by forced water cooling. Softened water is used for cooling. After being heated to a certain extent, the softened water can be used as water supply for the evaporator of the waste heat recovery device 34, thereby realizing the effective recovery of all the waste heat of the primary flue gas of the converter.

[0110] Fig.15 The overall structure of the converter primary flue gas purification system is shown schematically. Fig.15The converter primary flue gas purification system 1 is described in detail. The converter primary flue gas purification system 1 includes a converter and a vaporization cooling flue 11 connected to the output end of the converter. The output end of the vaporization cooling flue 11 is sequentially connected to 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. The output end of the switching valve 12 is connected to a gas tank 13 and a venting chimney 38 respectively. 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 provided in the converter primary flue gas purification system 1 are the same as those of the reduction system 5. The multi-stage flue gas filtration and purification device 52 is provided in the converter primary flue gas purification system 1 because the capacity of a single set of ultra-high temperature flue gas filtration and purification device 52 to process air volume is very limited. Multiple sets of devices can be connected in parallel to process ultra-high temperature flue gas with a large flue gas volume from converter steelmaking.

[0111] The technical scope of the present invention is not limited to the contents in the above description. Those skilled in the art can make various deformations and modifications to the above embodiments without departing from the technical idea of ​​the present invention, and these deformations and modifications should all fall within the protection scope of the present invention.

Claims

1. A converter primary flue gas dust ash resource utilization processing system, characterized in that: It comprises a converter primary flue gas purification system (1) and a dust removal ash treatment system (2) used in conjunction with each other, wherein the dust removal ash treatment system (2) receives dust removal ash from the converter primary flue gas purification system (1), separates and removes iron powder from the dust removal ash, and collects the iron powder; The dust ash treatment system (2) comprises a primary sorting oxidation system (3), a secondary sorting oxidation system (4) and a reduction system (5) which are connected in sequence. The primary sorting oxidation system (3) and the secondary sorting oxidation system (4) collect the magnetic fine powder in the dust ash after sorting and oxidation, and transport the magnetic fine powder to the reduction system (5) to complete the iron powder reduction process and collect the obtained iron powder.

2. The converter primary flue gas dust ash resource utilization processing system according to claim 1 is characterized in that: The primary separation 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) which are connected in sequence, and the second output ends of the first-stage micro-powder magnetic separation device (32) and the second-stage micro-powder magnetic separation device (32) are both connected to the reduction system (5); The input end of the first-stage fine powder magnetic separation device (32) is connected to the airflow fine powder mill (31), a waste heat recovery device (34) is further provided between the oxidation roasting furnace (33) and the second-stage fine powder magnetic separation device (32), and the first output end of the second fine powder magnetic separation device (32) is connected to the dust collector (35); The second output end of the dust collector (35) supplies tailings to the secondary separation oxidation system (4), and the first output end thereof is sequentially connected to a heat exchanger (36), a fan (37) and a dispersing chimney (38).

3. The converter primary flue gas dust resource utilization processing system according to claim 2 is characterized in that: The secondary separation oxidation system (4) comprises an air flow micro powder mill (31), an oxidation roasting furnace (33), a waste heat recovery device (34), a micro powder magnetic separation device (32), a dust collector (35), a heat exchanger (36), a fan (37) and a dissipation chimney (38) which are connected in sequence, and the second output end of the micro powder magnetic separation device (32) is connected to the reduction system (5); The secondary sorting 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 airflow micro-powder mills (31) in this group or the next group.

4. The converter primary flue gas dust ash resource utilization processing system according to claim 3 is characterized in that: The micro powder magnetic separation device (32) comprises a smoke and dust channel (32a-1) fixedly arranged in a vertical direction, and a plurality of separation components fixedly arranged close to the outer edge of the smoke and dust channel (32a-1), wherein the separation component consists of a magnetic rotating disk component (32a-2) and a discharge trough (32a-3), wherein the magnetic rotating disk component (32a-2) is fixedly arranged above the discharge trough (32a-3), and a cleaning device is fixedly arranged in the discharge trough (32a-3), wherein the cleaning device can contact the surface of the magnetic rotating disk, wherein there are a plurality of magnetic rotating disks, and the plurality of magnetic rotating disks 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 gas dust resource utilization processing system according to claim 3 is characterized in that: The micro-powder magnetic separation device (32) comprises a smoke inlet cavity (32b-1), a flow dividing 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 flow dividing cone shell (32b-2), and the upper end of the smoke outlet cavity (32b-4) extends into the lower end of the flow dividing cone shell (32b-2); A magnetic rod rack (32b-5) is arranged on the outer surface of the smoke inlet cavity (32b-1), the magnetic rod rack (32b-5) matches the shape of the smoke inlet cavity (32b-1), and a plurality of magnetic rods (32b-6) are fixedly arranged on the side of the magnetic rod rack (32b-5) facing the smoke inlet cavity (32b-1), and the magnetic rod rack (32b-5) is rotatably fixedly arranged on the outer surface of the smoke inlet cavity (32b-1).

6. The converter primary flue gas dust resource utilization processing system according to claim 1 is characterized in that: The reduction system (5) comprises a reduction roasting furnace (51), a flue gas filtering and purification device (52), a waste heat recovery device (34), a heat exchanger (36), a fan (37) and a dissipation chimney (38) which are connected in sequence. The reduction roasting furnace (51) receives the magnetic micropowder from the primary separation oxidation system (3) and the secondary separation oxidation system (4) and completes the reduction process of the magnetic micropowder.

7. The converter primary flue gas dust ash resource utilization processing system according to claim 6 is characterized in that: The smoke filtering and purifying device (52) comprises a dust removal housing (521) and a pneumatic conveying device (522) fixedly arranged below the dust removal housing (521) and used for conveying dust removal ash; An air inlet and an air outlet are provided on the dust removal shell (521), an air inlet box (523) is fixedly provided inside the dust removal shell (521) along the length direction of the air inlet, a plurality of axial cyclones (524) are fixedly provided in the air inlet box (523), a spray assembly (525) is fixedly provided above the axial cyclones (524); an evaporator assembly (526) is fixedly provided below the air inlet box (523).

8. The converter primary flue gas dust resource utilization processing system according to claim 7 is characterized in that: The axial cyclone (524) comprises a separation chamber (5241) fixedly arranged on the bottom plate of the air inlet box (523) and an air guide assembly fixedly arranged on the top plate of the air inlet box (523); The width of the air guide component is smaller than the width of the separation cavity (5241) on one side close to the air guide component, the air guide component and the separation cavity (5241) are located on the same axis, the lower end of the air guide component is embedded and fixed with the upper surface of the separation cavity (5241), and the air guide component and the separation cavity (5241) are connected; The air guide component includes 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 notch is provided at the upper end of the air guide sleeve (5242) for the ceramic fiber filter tube (5243) to be embedded and fixed; the ceramic fiber filter tube (5243) includes a rigid frame (5244), and a plurality of ventilation holes (5245) are opened on the rigid frame (5244); the outer edge of the rigid frame (5244) is coated with a ceramic fiber membrane (5246), and a baffle is fixedly provided at the upper end of the ceramic fiber filter tube (5243).

9. The converter primary flue gas dust resource utilization processing system according to claim 7 is characterized in that: A uniform unloading device (527) is also provided in the dust removal shell (521), and the uniform unloading device (527) includes a chute section (5271) fixed at equal intervals in the dust removal shell (521), a bottom support plate (5272) is fixedly provided in the gap area at a certain distance below the chute section (5271), and a nozzle (5273) is fixedly provided at the midpoint of the bottom support plate (5272).

10. The converter primary flue gas dust resource utilization processing system according to claim 1, characterized in that: The converter primary flue gas purification treatment system (1) comprises a converter and a vaporization cooling flue (11) connected to the output end of the converter, the output end of the vaporization cooling flue (11) is sequentially connected to a multi-stage flue gas filtering and purification device (52) as described in any one of claims 8 to 9, 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 connected to a gas tank (13) and a venting chimney (38).

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