CN218710619U - Direct reduction device for dedusting ash of steel plant - Google Patents
Direct reduction device for dedusting ash of steel plant Download PDFInfo
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- CN218710619U CN218710619U CN202222882155.5U CN202222882155U CN218710619U CN 218710619 U CN218710619 U CN 218710619U CN 202222882155 U CN202222882155 U CN 202222882155U CN 218710619 U CN218710619 U CN 218710619U
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Abstract
The utility model discloses a direct reduction device for dedusting ash of steel and iron plants, belonging to the field of dedusting ash treatment, comprising a batching system, a grinding system, a coal gas supply system, a dedusting system, a cyclone reduction system and a briquetting machine; the batching system conveys the mixed dedusting ash to the grinding system; the grinding system is connected with the cyclone reduction system in sequence; the coal gas supply system comprises a first-stage gas supply system, a second-stage gas supply system and a third-stage gas supply system; the first-stage air supply system and the second-stage air supply system comprise burners; the dust removal system comprises a primary dust collector and a secondary dust collector; the cyclone reduction system comprises a primary cyclone, a secondary cyclone and a tertiary cyclone; and the briquetting machine is used for briquetting the directly reduced iron dust particles discharged by the three-stage cyclone cylinder. Compared with the prior art have the characteristics that recovery efficiency is high.
Description
Technical Field
The utility model relates to a dedusting ash recycling technology, in particular to a dedusting ash direct reduction process for steel plants.
Background
The existing dust removal ash treatment process of the steel plant comprises a rotary kiln and a rotary hearth furnace, wherein coke powder is respectively used as a reducing agent, calcination reduction is carried out in the rotary kiln or the rotary hearth furnace, and the reduced product comprises ZnO and direct reduced iron. For example, in a recovery processing method of iron-containing fly ash in ferrous metallurgy (CN 114934171A) and a reduction utilization method of stainless steel fly ash (CN 101705333A), a mixture of fly ash, a reducing agent and a binding agent is added from the tail of a rotary kiln, and reduction volatilization roasting is carried out after passing through a preheating zone, a high-temperature reducing zone and a cooling zone in the kiln, so as to form iron-rich kiln slag with a certain reduction rate and discharge the iron-rich kiln slag out of the kiln, and zinc-rich smoke dust is collected.
However, the above process has the following disadvantages:
(1) In the rotary kiln, the mixture is formed into a certain thickness, the filling rate is about 15%, and natural air for combustion is provided by a kiln head Roots blower and a kiln tail main exhaust fan. Oxygen in the air needs to penetrate through the material layer to enter the interior of the material layer to react with the coke powder to generate CO in an oxygen-deficient environment, and the excessive CO is wrapped around the ferric oxide to realize the one-step reduction of the ferric oxide. This requires that the layer not be too thick to prevent oxygen from entering, but too thin to prevent the oxidizing atmosphere from hindering the reduction of the metallic iron. The temperature in the kiln is extremely difficult to control in the actual production operation, and the local temperature of materials in the kiln is often overhigh to 1300-1400 ℃ due to uneven material distribution or temperature field distribution fluctuation, so that the SiO in the ash content in FeO and coke powder in the kiln is caused 2 、Al 2 O 3 The reaction forms lumps and rings, which cause frequent production interruptions and only 30 days of campaign.
(2) The kiln tail flue gas contains chlorides volatilized from about 400 ℃, znO, pbO and other valuable element gases volatilized from 900-1100 ℃, and various compounds are mixed at the kiln tail, so that the purity of the valuable elements is reduced, the quality and grade of the product are poor, the economic value of the product is influenced, and the cost of the subsequent purification process is increased.
In the rotary hearth furnace process, the converter gas is used for heating and calcining after the pellets are pressed, although the calcining temperature of each zone can be controlled more accurately, the process and equipment are complex, only dust with low zinc content can be treated, and the limitation is large. Meanwhile, the problem of low purity of valuable elements in kiln tail flue gas exists.
SUMMERY OF THE UTILITY MODEL
The technical task of the utility model is not enough to above prior art, provides a dust removal ash direct reduction technology of steel and iron plant, then through tertiary direct reduction cyclone, will reduce gas and superfine dust raw materials mixture, reduce under the temperature that reaches the settlement.
The technical proposal of the utility model for solving the technical problem is that: the utility model provides a dust removal ash direct reduction device of steel plant which characterized in that: the device comprises a batching system, a grinding system, a coal gas supply system, a dust removal system, a cyclone reduction system and a briquetting machine; the batching system conveys the mixed dedusting ash to the grinding system; the grinding system is connected with the cyclone reduction system in sequence; the coal gas supply system comprises a first-stage gas supply system, a second-stage gas supply system and a third-stage gas supply system; the first-stage air supply system and the second-stage air supply system comprise burners; the dust removal system comprises a primary dust collector and a secondary dust collector; the cyclone reduction system comprises a primary cyclone, a secondary cyclone and a tertiary cyclone; the feeding port of the primary cyclone cylinder is connected with a primary air supply system, and the top of the primary cyclone cylinder is connected with a primary dust collector; the feeding port of the secondary cyclone cylinder is connected with a secondary air supply system, and a chute at the lower end of the primary cyclone cylinder is communicated with the side wall of the secondary air supply system; the top of the secondary cyclone cylinder is connected with a secondary dust collector; the feeding port of the tertiary cyclone cylinder is connected with a tertiary air supply system, and a chute at the lower end of the secondary cyclone cylinder is communicated with the side wall of the tertiary air supply system; the top of the third-stage cyclone is sequentially connected with a waste heat boiler and a second-stage dust collector; the three cyclones are all provided with temperature detection devices; and the briquetting machine is used for briquetting the directly reduced iron dust particles discharged by the three-stage cyclone cylinder.
Further, still include waste heat recovery device.
In the optimization selection, the waste heat recovery device is a waste heat boiler.
Furthermore, the batching system comprises a raw material batching bin, a weighing scale, a mixed material conveyor and a bucket lifter.
Further, the grinding system comprises a ball mill, a discharging device and a ventilating dust remover; the lifter of the batching system is connected with the tail of the ball mill, the ground dust enters the three-stage cyclone reduction system through the chute at the head of the mill, and the chute at the head of the ball mill is communicated with the side wall of the first-stage gas supply system.
Further, the first-stage gas supply system is internally provided with a first-stage reducing gas, the second-stage gas supply system is internally provided with a second-stage mixed reducing gas, and the third-stage gas supply system is internally provided with a third-stage mixed reducing gas.
Further, the primary reducing gas is coke oven gas, the secondary mixed reducing gas is the mixture of natural gas and coke oven gas, and the tertiary mixed reducing gas is the mixture of hydrogen and coke oven gas.
Further, the top of the secondary cyclone cylinder is sequentially connected with a waste heat boiler and a secondary dust collector; the top of the three-stage cyclone cylinder is sequentially connected with a waste heat boiler and a secondary dust collector.
Furthermore, the temperature detection devices are uniformly distributed around the inlet and the outlet of each cyclone of the cyclone reduction system.
Furthermore, the periphery of the lower conical part of the first-stage cyclone cylinder, the second-stage cyclone cylinder and the third-stage cyclone cylinder of the cyclone reduction system is provided with blowing pipes, the blowing pipes are connected with the gas supply system at the corresponding level, and the gas in the blowing pipes is the reduction gas at the corresponding level.
Compared with the prior art, the utility model discloses following outstanding beneficial effect has:
1. the utility model mixes the reducing gas with the superfine dust raw material through the cyclone, and reduces the reducing gas at the set temperature, thereby avoiding roasting, directly reducing the reducing gas below the melting point of the raw material, and avoiding the problems of ring formation, caking and the like caused by inaccurate temperature control of the rotary kiln and the rotary hearth furnace;
2. the ash content brought by the solid reducing agent is reduced to form a low-melting-point compound, so that the production operation rate is improved;
3. and the three-stage cyclone reduction is adopted, the reaction temperature at each stage is accurately controlled, the reaction stage and reaction products are accurately controlled, the formation of a local metal iron liquid phase and the fusion of impurity metals are avoided, various valuable elements in wide raw materials are accurately purified, the formed direct reduction particles are purer in quality, and the utilization value of the dedusting ash raw material is greatly improved.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic flow chart of the present invention.
Detailed Description
The invention is further described with reference to the drawings and the detailed description. In the following, only certain exemplary embodiments are briefly described. As those skilled in the art will recognize, the described embodiments may be modified in various different ways, all without departing from the spirit or scope of the claimed embodiments. Accordingly, the drawings and description are to be regarded as illustrative in nature, and not as restrictive.
In the following embodiments, unless otherwise explicitly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly, e.g., as being permanently connected, removably connected, or integral; the connection can be mechanical connection, electrical connection or communication; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meanings of the above terms in the embodiments of the present invention can be understood by those skilled in the art according to specific situations.
It is to be understood that the terms "central," "longitudinal," "transverse," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," "end," "side," and the like are used in an illustrative and non-restrictive sense, and are used in a generic and descriptive sense only and not for purposes of limitation, the referenced devices or elements must be in a particular orientation, configuration or operation, and not for purposes of limitation, as the orientation or positional relationship is illustrated in the figures.
This the utility model discloses a further grinding improves its fineness and activity to the dust removal ash, then through tertiary direct reduction whirlwind section of thick bamboo, will reduce gas and superfine dust raw materials and mix, reduces under reaching the temperature of settlement, through meticulous control reduction temperature, distinguishes reduction product, improves valuable element's grade, promotes economic value. Meanwhile, the reaction temperature and speed of the direct reduced iron can be controlled, the direct reduction is carried out below the melting point of the raw materials, and the problems of ring formation, caking and the like caused by inaccurate temperature control of the rotary kiln and the rotary hearth furnace are avoided.
As shown in fig. 1 and 2, the utility model comprises a material distribution system, a grinding system 2, a cyclone reduction system, a coal gas supply system, a waste heat recovery device 5, a dust removal system and a briquetting machine 7.
The batching system comprises a raw material batching bin 11, a weighing scale, a mixed material conveyor 12 and a bucket elevator 13. The steel dust is accurately weighed according to a set proportion and then is gathered into a belt of a mixed material conveyor 12, and the belt is conveyed to a bucket elevator 13 to convey the mixed dust to a grinding system 2.
The grinding system 2 comprises a ball mill. And a bucket lift 13 of the batching system is connected with the tail of the ball mill, and the ground dust enters the cyclone reduction system through a chute at the head of the ball mill. The entered fly ash mixture is subjected to step-by-step grinding and crushing by a ball mill to form superfine dust with fineness of more than 400 meshes, the ground dust is subjected to crystal internal cracks increase inside dust particles while crushing the large particles of the original fly ash, more holes are formed, the gas entering is facilitated to carry out reduction reaction, the gas discharge after oxidation is facilitated, and the reaction activity of the fly ash particles is greatly increased. In the optimization scheme, the ball mill is provided with a discharging ventilating dust remover.
The gas supply system comprises a primary gas supply system 41, a secondary gas supply system 42 and a tertiary gas supply system 43.
The first-stage gas supply system 41 is internally provided with a first-stage reducing gas, in particular coke oven gas. A burner is included in the first stage air supply system 41.
The second-stage gas supply system 42 is internally provided with a second-stage mixed reducing gas, specifically a mixture of natural gas and coke oven gas, so as to ensure that the temperature in the second-stage cyclone 32 reaches 900-1000 ℃. The method specifically comprises the following steps: the initial setting ratio of the natural gas to the coke oven gas is 1, and the natural gas adding ratio is adjusted according to the temperature condition in the process. The ratio of natural gas and coke oven gas is controlled by a flow valve of a pipeline system, and a flow meter is arranged at the front end of the valve to measure the flow. If the temperature of the system is insufficient, the consumption of the natural gas is gradually increased, the gas proportion can be stably used when the temperature is increased to reach the set 900 ℃, the natural gas proportion is reduced when the temperature is too high, and the temperature of each part in the cylinder (the whole part from the inlet to the outlet of the cyclone cylinder) is accurately controlled within the temperature requirement. The second stage air supply system 42 includes a burner therein.
The third-stage gas supply system 43 is internally provided with three-stage mixed reducing gas, specifically the mixture of hydrogen and coke oven gas, and the pressure is 2-3MPa, so as to ensure that the temperature in the third-stage cyclone cylinder 33 reaches 1000-1200 ℃. The method specifically comprises the following steps: the initial setting ratio of the hydrogen to the coke oven gas is 3, and in the process, the adding proportion of the coke oven gas is adjusted according to the temperature condition in the three-stage cyclone cylinder 33. If the temperature of the system is insufficient, the using amount of the coke oven gas is gradually reduced, the gas proportion can be stably used when the temperature is increased to reach the set 900 ℃, the using proportion of the coke oven gas is increased when the temperature is too high, and then the temperature of each part in the cylinder (the whole part from the inlet to the outlet of the cyclone cylinder) is accurately controlled within the temperature requirement, so that the reduction efficiency is ensured.
The dust removal system comprises a primary dust collector 61 and a secondary dust collector 62.
The cyclone reduction system comprises a primary cyclone 31, a secondary cyclone 32 and a tertiary cyclone 33.
The feeding port of the primary cyclone cylinder 31 is connected with a primary air supply system 41, and the chute at the head of the ball mill is communicated with the side wall of the primary air supply system 41. The top of the primary cyclone cylinder 31 is connected with a primary dust collector 61. The first stage cyclone reduction is realized in the first stage cyclone cylinder 31: the first-stage gas supply system 41 injects coke oven gas into the burner through the high-speed burner, and the pulverized fly ash dust is injected into the cyclone by the high-temperature and high-pressure oxidizing gas generated by the burner. The gas temperature in the primary cyclone 31 is guaranteed to reach about 500 ℃ by accurately controlling the flow of the gas supply system. The dust is heated and reduced by primary reducing gas (coke oven gas) in the primary cyclone cylinder 31 and is settled to the bottom of a cone, znCl, alkali metal oxide and other volatile chlorides generated by mixing clean tail gas are led out to the primary dust collector 61 through a top exhaust pipe of the cyclone cylinder, and are collected by multi-pipe heat dissipation of the primary dust collector 61, and the collected chlorides and alkali metal oxide can be further purified by a water washing system and a triple effect evaporation system.
The feeding port of the secondary cyclone cylinder 32 is connected with the secondary air supply system 42, and the chute at the lower end of the primary cyclone cylinder 31 is communicated with the side wall of the secondary air supply system 42. The top of the secondary cyclone cylinder 32 is connected with the waste heat recovery device 5 and the secondary dust collector 62 in sequence. The waste heat recovery device 5 can be a waste heat boiler. The second stage cyclone reduction is realized in the second stage cyclone 32: the preheated and primarily purified dust-removing ash collected from the primary cyclone cylinder 31 is blown into the secondary cyclone cylinder 32 by high-temperature and high-pressure secondary reducing gas (mixture of natural gas and coal gas), and then is heated to 900-1000 ℃, wherein ZnO is reduced into metal Zn by C contained in the dust-removing ash and CO in the incompletely combusted reducing gas, under the condition of the temperature, the reduction and evaporation speed of ZnO is fast, the reaction time is extremely short, the reacted metal Zn steam is guided into the waste heat recovery device 5 and the secondary dust collector 62 to be collected, and because the whole system maintains better reducing atmosphere, the oxidation amount of the metal Zn is lower than that of a smoke system of a rotary kiln and a rotary hearth furnace, and the purity of the metal Zn is higher.
The third stageThe feeding port of the cyclone cylinder 33 is connected with a third stage air supply system 43, and a chute at the lower end of the second stage cyclone cylinder 32 is communicated with the side wall of the third stage air supply system 43. The top of the third-stage cyclone 33 is connected with a waste heat boiler. The bottom of the three-stage cyclone cylinder 33 is connected with the briquetting machine 7. And the third-stage cyclone reduction is realized in the third-stage cyclone cylinder 33: the third gas supply system 43 directly sprays the high-pressure third reducing gas (hydrogen and coke oven gas) and the partially reduced dust collected from the second cyclone 32 into the third cyclone 33 without using a burner, the temperature in the third cyclone is 1000-1200 ℃, the high-pressure third reducing gas (hydrogen and coke oven gas) reacts with the iron oxide in the high-temperature dust particles, and after oxygen is deprived, metal Fe and CO are formed 2 、H 2 And (O). The tail gas is led out to a waste heat boiler through a gas conduit at the top of the tertiary cyclone cylinder 33, and then enters a secondary dust collector 62 to further collect evaporated Zn metal. The formed direct reduced iron particles are collected from the bottom of the tertiary cyclone 33 into the briquetting machine 7. The temperature in the cylinder is 1000-1200 ℃, which is lower than the temperature of the reaction of gangue (containing silicon dioxide, calcium oxide, aluminum oxide, magnesium oxide and other compound parts) in the dust removal ash and ferrous iron.
The three cyclones are all provided with temperature detection devices, specifically four temperature detection devices are uniformly distributed around the inlets and outlets of the cyclones. And temperature detection probes are distributed so as to accurately feed back the reaction temperature. When the reduction temperature in the cyclone is insufficient or the reduction atmosphere is insufficient, the metallization rate is low, the production efficiency and the process cost requirements are considered, the metallization rate is controlled not to be too high, and the reduction speed of zinc oxide and iron oxide is high under the condition of reaching the reduction temperature and the reduction atmosphere. And the balance of metallization rate, reduction speed, production efficiency and process cost can be realized in the temperature control range.
In the optimized scheme, the periphery of the lower conical part of the three cyclones is distributed with the injection pipes 34, the injection pipes 34 are connected with the corresponding grade of gas supply system, and the gas in the injection pipes 34 is the reducing gas with the corresponding grade. The blowing pipes 34 and the inner wall of the conical barrel form an angle of 25-35 degrees, the optimized scheme is 30 degrees, the blown air flow and the materials are ensured to continuously keep rotating and suspending the whole, the flow of the reducing gas can be controlled by adjusting the angle and the flow of the coal gas of each layer of blowing pipes 34, so that the materials at the conical part are gradually reduced according to the designed speed, and the reduction time of the dust is controlled. The falling time of the materials is adjusted, endothermic reaction can be resisted in the whole reduction process, and the inlet and outlet temperature and the highest temperature in the cyclone are controlled. In fig. 1, the piping of the connection portion of the blowing pipe 34 and the corresponding level of the gas supply system is omitted for the sake of simplification of the structure.
The briquetting machine 7 is used for briquetting and spraying water mist cooling of the directly reduced iron dust particles discharged by the three-stage cyclone 33, so that the internal metal iron is not oxidized by the atmosphere and is convenient to transport and use.
In the optimization scheme, the briquetting machine 7 is sequentially connected with the conveying system.
It should be noted that while the invention has been described in detail with respect to specific embodiments thereof, it will be apparent to those skilled in the art that various obvious changes can be made therein without departing from the spirit and scope of the invention.
Claims (10)
1. The utility model provides a dust removal ash direct reduction device of steel plant which characterized in that: the device comprises a batching system, a grinding system, a coal gas supply system, a dust removal system, a cyclone reduction system and a briquetting machine;
the batching system conveys the mixed dedusting ash to the grinding system;
the grinding system is connected with the cyclone reduction system in sequence;
the coal gas supply system comprises a first-stage gas supply system, a second-stage gas supply system and a third-stage gas supply system; the first-stage air supply system and the second-stage air supply system comprise burners;
the dust removal system comprises a primary dust collector and a secondary dust collector;
the cyclone reduction system comprises a primary cyclone, a secondary cyclone and a tertiary cyclone; the feeding port of the primary cyclone cylinder is connected with a primary air supply system, and the top of the primary cyclone cylinder is connected with a primary dust collector; the feeding port of the secondary cyclone cylinder is connected with a secondary air supply system, and a chute at the lower end of the primary cyclone cylinder is communicated with the side wall of the secondary air supply system; the top of the secondary cyclone cylinder is connected with a secondary dust collector; the feeding port of the third cyclone cylinder is connected with a third air supply system, and a chute at the lower end of the second cyclone cylinder is communicated with the side wall of the third air supply system; the top of the third-stage cyclone is sequentially connected with a waste heat boiler and a second-stage dust collector; the three cyclones are all provided with temperature detection devices;
and the briquetting machine is used for briquetting the directly reduced iron dust particles discharged by the three-stage cyclone cylinder.
2. The direct reduction device for the dedusting ash of the steel plant according to the claim 1, is characterized in that: still include waste heat recovery device.
3. The direct reduction device for the dedusting ash of the steel plant according to the claim 2, is characterized in that: the waste heat recovery device is a waste heat boiler.
4. The direct reduction device for the dedusting ash of the steel plant according to the claim 1, is characterized in that: the batching system comprises a raw material batching bin, a metering scale, a mixed material conveyor and a bucket lifter.
5. The direct reduction device for the fly ash of the steel and iron plant according to claim 1, characterized in that: the grinding system comprises a ball mill, a discharging and ventilating dust remover; the lifter of the batching system is connected with the tail of the ball mill, the ground dust enters the three-stage cyclone reduction system through the chute at the head of the mill, and the chute at the head of the ball mill is communicated with the side wall of the first-stage gas supply system.
6. The direct reduction device for the dedusting ash of the steel plant according to the claim 1, is characterized in that: the first-stage gas supply system is internally provided with a first-stage reducing gas, the second-stage gas supply system is internally provided with a second-stage mixed reducing gas, and the third-stage gas supply system is internally provided with a third-stage mixed reducing gas.
7. The direct reduction device for the dedusting ash of the steel plant according to the claim 6, is characterized in that: the primary reducing gas is coke oven gas, the secondary mixed reducing gas is the mixture of natural gas and coke oven gas, and the tertiary mixed reducing gas is the mixture of hydrogen and coke oven gas.
8. The direct reduction device for the dedusting ash of the steel plant according to the claim 1, is characterized in that: the top of the secondary cyclone cylinder is sequentially connected with a waste heat boiler and a secondary dust collector; the top of the three-stage cyclone cylinder is sequentially connected with a waste heat boiler and a secondary dust collector.
9. The direct reduction device for the dedusting ash of the steel plant according to the claim 1, is characterized in that: the temperature detection devices are uniformly distributed around the inlets and outlets of the cyclones of the cyclone reduction system.
10. The direct reduction device for the dedusting ash of the steel plant according to the claim 1, is characterized in that: and blowing pipes are distributed around the conical parts at the lower parts of the primary cyclone cylinder, the secondary cyclone cylinder and the tertiary cyclone cylinder of the cyclone reduction system, the blowing pipes are connected with the gas supply system at the corresponding level, and the gas in the blowing pipes is the reduction gas at the corresponding level.
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| CN202222882155.5U CN218710619U (en) | 2022-10-31 | 2022-10-31 | Direct reduction device for dedusting ash of steel plant |
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| CN202222882155.5U CN218710619U (en) | 2022-10-31 | 2022-10-31 | Direct reduction device for dedusting ash of steel plant |
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