CN111270077B - System and method for disposing dust collection ash of steel plant by using chain plate type high-temperature reduction furnace - Google Patents
System and method for disposing dust collection ash of steel plant by using chain plate type high-temperature reduction furnace Download PDFInfo
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- RNWHGQJWIACOKP-UHFFFAOYSA-N zinc;oxygen(2-) Chemical compound [O-2].[Zn+2] RNWHGQJWIACOKP-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/02—Working-up flue dust
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/2406—Binding; Briquetting ; Granulating pelletizing
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/248—Binding; Briquetting ; Granulating of metal scrap or alloys
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B13/00—Obtaining lead
- C22B13/02—Obtaining lead by dry processes
- C22B13/025—Recovery from waste materials
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/30—Obtaining zinc or zinc oxide from metallic residues or scraps
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/34—Obtaining zinc oxide
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B5/00—General methods of reducing to metals
- C22B5/02—Dry methods smelting of sulfides or formation of mattes
- C22B5/10—Dry methods smelting of sulfides or formation of mattes by solid carbonaceous reducing agents
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- C22B5/00—General methods of reducing to metals
- C22B5/02—Dry methods smelting of sulfides or formation of mattes
- C22B5/16—Dry methods smelting of sulfides or formation of mattes with volatilisation or condensation of the metal being produced
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/001—Dry processes
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Abstract
Description
技术领域technical field
本发明属于冶金工业固体废弃物的综合利用技术领域，尤其属于一种链板式高温还原炉处置钢铁厂收尘灰系统及方法。The invention belongs to the technical field of comprehensive utilization of solid waste in the metallurgical industry, in particular to a chain-plate type high-temperature reduction furnace disposal system and method for collecting dust in iron and steel plants.
背景技术Background technique
钢铁厂收尘灰包括长流程企业产生的高炉灰、转炉灰和短流程企业产生的电炉灰，产废量约占钢铁产量3％-5％，2017年我国电炉钢产能达1.4亿吨，约产生280万吨电炉粉尘。这种收尘灰铁含量通常达到35-55％以上，若直接返回高炉利用，会在高炉内产生锌的循环和富集，危害高炉生产；收尘灰中锌含量5-30％，铅含量1-4％，氯含量4％左右，若以传统方式填埋弃置，则会污染环境，危害人体健康。钢铁厂收尘灰是具有很高回收价值的二次资源，但同时也是钢铁行业目前最难处置的工业固废之一，尤其是电炉灰，根据《国家危险废物名录》(2018版)，电炉灰被归入含铅废物类管理，危废代码HW31(312-001-31)。如果能把收尘灰中的金属铁和锌分离出来并实现综合利用，将具有重要的经济价值。因此开展对收尘灰的回收利用，不仅可以使宝贵的资源得到充分利用，还可以减少其对环境的污染。Dust collected by iron and steel plants includes blast furnace ash, converter ash and electric furnace ash produced by short-process enterprises. The waste production accounts for about 3%-5% of steel output. In 2017, my country's electric furnace steel production capacity reached 140 million tons, about Generate 2.8 million tons of electric furnace dust. The iron content of this dust collection ash usually reaches more than 35-55%. If it is directly returned to the blast furnace for use, zinc circulation and enrichment will occur in the blast furnace, which will endanger the production of the blast furnace; the zinc content in the dust collection dust is 5-30%, and the lead content 1-4%, and the chlorine content is about 4%. If it is disposed of in a traditional landfill, it will pollute the environment and endanger human health. Dust collected from iron and steel plants is a secondary resource with high recycling value, but it is also one of the most difficult industrial solid wastes in the iron and steel industry, especially electric furnace ash. According to the "National List of Hazardous Wastes" (2018 Edition), electric furnace The ash is classified as lead-containing waste management, hazardous waste code HW31 (312-001-31). If the metal iron and zinc in dust collection can be separated and realized comprehensive utilization, it will have important economic value. Therefore, the recycling of dust collection can not only make full use of precious resources, but also reduce its pollution to the environment.
目前，对钢铁厂收尘灰的回收主要有火法和湿法两种。湿法工艺流程长，生产效率低，特别是废水排放量大，易产生二次污染，同时对成分要求高，多数收尘灰很难达到，处置成本高。火法工艺中，主要是采用回转窑高温还原挥发工艺，其有价金属回收率低，由于收尘灰中铁含量高，煅烧时窑内液相量大，容易结块，严重影响回转窑的生产运行；同时产品质量差，燃料消耗大，能量利用率低。近年来火法工艺采用转底炉或微波炉等新工艺和设备，由于设备造价高、采用燃气或者电能为能源、生产成本较高，没有获得有效推广。At present, there are mainly two methods of recycling dust from iron and steel plants: fire method and wet method. The wet process is long, the production efficiency is low, especially the waste water discharge is large, and it is easy to cause secondary pollution. At the same time, it has high requirements on the ingredients, and most of the dust collection is difficult to achieve, and the disposal cost is high. In the fire process, the high-temperature reduction and volatilization process of the rotary kiln is mainly used, and the recovery rate of valuable metals is low. Due to the high iron content in the dust collection ash, the liquid phase in the kiln is large during calcination, and it is easy to agglomerate, which seriously affects the production of the rotary kiln. operation; at the same time, the product quality is poor, the fuel consumption is large, and the energy utilization rate is low. In recent years, new technology and equipment such as rotary hearth furnace or microwave oven have been adopted in the pyrotechnic process. Due to the high cost of equipment, the use of gas or electric energy as energy, and high production costs, it has not been effectively promoted.
发明专利CN 106191453 B公开了一种利用转底炉尘灰回收锌富集物和氯化钾的方法，该方法首先将转底炉尘灰用水浸润，然后进行浆化和浸提，将浸提后的浆液固液分离，将得到的固体再进行洗涤和干燥，该专利中采用湿法处理转底炉尘灰，其生产效率较低，废水排放量大。Invention patent CN 106191453 B discloses a method for recovering zinc concentrate and potassium chloride by using dust from a rotary hearth furnace. In this method, the dust from a rotary hearth furnace is soaked in water first, and then pulped and leached. The final slurry is separated from solid and liquid, and the obtained solid is washed and dried. In this patent, the wet method is used to treat the dust of the rotary hearth furnace, which has low production efficiency and large wastewater discharge.
发明专利CN 102899505 A公布了一种利用回转窑回收锌的方法及装置，通过将高炉灰、电炉灰、无烟煤和瓦斯泥混合后送入回转窑高温燃烧，使锌形成气化锌，然后将气化锌降温的同时除去灰尘，将气化锌降温后在空气中氧化，然后送入收尘室回收。该方法回收锌效率低，而高炉灰和电炉灰中铁含量高，煅烧时窑内液相量大，容易结块，严重影响回转窑的生产运行。Invention patent CN 102899505 A discloses a method and device for recovering zinc by using a rotary kiln. By mixing blast furnace ash, electric furnace ash, anthracite and gas mud and sending them into the rotary kiln for high-temperature combustion, zinc is formed into gasified zinc, and then the gas is Dust is removed while the zinc oxide is cooling down. After the zinc oxide is cooled down, it is oxidized in the air, and then sent to the dust collection room for recovery. The zinc recovery efficiency of this method is low, and the iron content in the blast furnace ashes and electric furnace ashes is high, and the liquid phase in the kiln is large during calcination, which is easy to agglomerate, which seriously affects the production and operation of the rotary kiln.
上述两种方法生产效率较低，能耗成本高，而且收尘灰中的锌没有得到有效地回收，回收过程中容易产生二次污染。The production efficiency of the above two methods is low, the energy consumption cost is high, and the zinc in the dust collecting dust has not been effectively recovered, and secondary pollution is likely to be generated during the recovery process.
发明内容Contents of the invention
为了克服现有技术中的问题，本发明提供一种链板式高温还原炉处置钢铁厂收尘灰系统及方法，在满足环保和安全生产的前提下将钢铁厂收尘灰进行磨浸洗涤后进行成球造粒，经过蒸发脱水、预热和高温还原，使收尘灰中的铅锌组分得以挥发进入烟气，再经氧化获得含有氧化锌和氧化铅粉的烟气，最后通过收尘灰从烟气中回收氧化锌和氧化铅粉，经过烧结获得的炉渣经过冷却、粉碎、磁选回收铁粉，剩余炉渣作为建筑材料原料，从而实现无害化、资源化处置钢铁厂收尘灰，完全消除二次污染风险，安全生产。In order to overcome the problems in the prior art, the present invention provides a chain-plate type high-temperature reduction furnace treatment system and method for collecting dust in iron and steel plants. Under the premise of meeting environmental protection and safe production, the dust collected in iron and steel plants is ground, soaked and washed. Ball granulation, after evaporation and dehydration, preheating and high-temperature reduction, the lead and zinc components in the dust collection ash can be volatilized into the flue gas, and then oxidized to obtain flue gas containing zinc oxide and lead oxide powder, and finally through dust collection Zinc oxide and lead oxide powder are recovered from flue gas, the slag obtained by sintering is cooled, pulverized, and magnetically separated to recover iron powder, and the remaining slag is used as raw material for building materials, so as to realize harmless and resourceful disposal of steel plant dust collection , Completely eliminate the risk of secondary pollution, safe production.
为了实现上述目的，本发明通过以下技术方案实现：In order to achieve the above object, the present invention is achieved through the following technical solutions:
一种链板式高温还原炉处置钢铁厂收尘灰系统，包括洗涤脱氯系统、成球造粒系统、挥发提锌系统和烟气处理系统；所述洗涤脱氯系统、成球造粒系统和挥发提锌系统依次相连，所述烟气处理系统与挥发提锌系统相连，系统内的装置均采用密封装置，并设置抽吸机用于形成微负压；所述挥发提锌系统包括依次连接的链板式高温还原炉、氧化室、盐水蒸发与烟气沉降机、高温静电收尘器和固体库，所述高温静电收尘器通过排风机与链板式高温还原炉相连。A chain-plate type high-temperature reduction furnace disposal system for dust collection in iron and steel plants, including a washing and dechlorination system, a pelletizing and granulating system, a volatile zinc extraction system and a flue gas treatment system; the washing and dechlorination system, the pelletizing and granulating system and The volatilization zinc extraction system is connected sequentially, the flue gas treatment system is connected with the volatilization zinc extraction system, the devices in the system are all sealed devices, and a suction machine is set to form a slight negative pressure; the volatilization zinc extraction system includes sequential connection Chain-plate type high-temperature reduction furnace, oxidation chamber, brine evaporation and flue gas settling machine, high-temperature electrostatic precipitator and solid storage. The high-temperature electrostatic precipitator is connected with chain-plate type high-temperature reduction furnace through exhaust fan.
进一步地，所述链板式高温还原炉包括炉体和由炉体包裹所形成的空腔，所述空腔由蒸发预热部、高温还原部和冷却部组成。Further, the chain-plate type high-temperature reduction furnace includes a furnace body and a cavity formed by wrapping the furnace body, and the cavity is composed of an evaporation preheating part, a high-temperature reduction part and a cooling part.
进一步地，所述蒸发预热部和冷却部位于炉体一侧，所述高温还原部位于炉体另一侧，所述蒸发预热部位于冷却部上方，所述蒸发预热部和冷却部之间设有烟气室，所述蒸发预热部、高温还原部和冷却部分别设有第一链板机、第二链板机和第三链板机。Further, the evaporation preheating part and cooling part are located on one side of the furnace body, the high temperature reduction part is located on the other side of the furnace body, the evaporation preheating part is located above the cooling part, and the evaporation preheating part and cooling part There is a flue gas chamber between them, and the evaporation preheating part, the high temperature reduction part and the cooling part are respectively provided with a first chain plate machine, a second chain plate machine and a third chain plate machine.
进一步地，所述蒸发预热部上部设有第一进料口和第一烟气出口，下部设有至少一台第一链板机。Further, the upper part of the evaporation preheating part is provided with a first feed inlet and a first flue gas outlet, and the lower part is provided with at least one first chain conveyor.
进一步地，所述蒸发预热部与高温还原部相连通，其连通处设有第二进料口。Further, the evaporation preheating part communicates with the high-temperature reducing part, and a second feed port is provided at the connecting part.
进一步地，所述高温还原部上部设有第二烟气出口，中部设有至少一台第二链板机，下部设有集灰斗，集灰斗下部设有至少一个第一出灰口，所述第一出灰口与固体渣库相连。Further, the upper part of the high-temperature reduction part is provided with a second flue gas outlet, the middle part is provided with at least one second chain conveyor, the lower part is provided with an ash collecting hopper, and the lower part of the ash collecting hopper is provided with at least one first ash outlet, The first ash outlet is connected with the solid slag storage.
进一步地，所述高温还原部与冷却部相连通，其连通处设有第三进料口。Further, the high-temperature reducing part is connected to the cooling part, and a third feeding port is provided at the connecting part.
进一步地，所述高温还原部设有燃料喷嘴，数量至少一个，所述燃料喷嘴安装于第二链板机的上方炉体处。Further, the high-temperature reducing part is provided with at least one fuel nozzle, and the fuel nozzle is installed at the upper furnace body of the second chain conveyor.
进一步地，所述高温还原部第二链板机的外部设有密封气室，所述密封气室为长方体结构，侧面设有多个高压空气进气孔，上部设有至少一个排气孔。Furthermore, a sealed air chamber is provided on the outside of the second chain plate machine in the high-temperature reduction part, and the sealed air chamber is a cuboid structure with multiple high-pressure air inlet holes on the side and at least one exhaust hole on the upper part.
进一步地，所述冷却部上部设有出风口，下部设有至少一个充气室，中部设有至少一台第三链板机，所述第三链板机物料下落处设有出料口。Further, the upper part of the cooling part is provided with an air outlet, the lower part is provided with at least one air-filled chamber, the middle part is provided with at least one third chain conveyor, and the third chain conveyor is provided with a material outlet.
进一步地，每个充气室底部设有第二出灰口，侧壁上设有进风口，不同充气室之间设有隔墙。Furthermore, a second ash outlet is provided at the bottom of each plenum chamber, an air inlet is provided on the side wall, and partition walls are provided between different plenum chambers.
进一步地，所述第二出灰口与固体渣库相连。Further, the second ash outlet is connected with the solid slag storage.
进一步地，所述第一链板机、第二链板机、第三链板机与炉体顶面的距离为链板机宽度的0.3～1倍。Further, the distance between the first chain conveyor, the second chain conveyor, and the third chain conveyor and the top surface of the furnace body is 0.3 to 1 times the width of the chain conveyor.
进一步地，所述第一链板机、第二链板机和第三链板机的数量分别为2台或2台以上时，第一链板机与第一链板机之间、第二链板机与第二链板机之间或第三链板机与第三链板机之间的距离为链板机宽度的0.3～1倍。Further, when the number of the first chain plate machine, the second chain plate machine and the third chain plate machine is 2 or more respectively, between the first chain plate machine and the first chain plate machine, the second The distance between the chain conveyor and the second chain conveyor or between the third chain conveyor and the third chain conveyor is 0.3 to 1 times the width of the chain conveyor.
进一步地，所述第一链板机、第二链板机和第三链板机运行链板上粘贴有耐火材料层。Further, the running chain plates of the first chain conveyor, the second chain conveyor and the third chain conveyor are pasted with refractory material layers.
进一步地，所述炉体长度≤30m，宽度≤5m，Further, the length of the furnace body is ≤30m, and the width is ≤5m,
进一步地，所述烟气室为倒喇叭形，下部开口与冷却部相连，中部设有热烟气进口。Further, the flue gas chamber is in the shape of an inverted trumpet, the lower opening is connected with the cooling part, and the middle part is provided with a hot flue gas inlet.
进一步地，所述炉体的机壳包括钢制机壳本体、覆盖在机壳本体上的保温材料层和覆盖在保温材料层上的耐火砖层，所述保温材料层与耐火砖层用钯钉固定在机壳上。Further, the casing of the furnace body includes a steel casing body, an insulating material layer covering the casing body and a refractory brick layer covering the insulating material layer, and the insulating material layer and the refractory brick layer are made of palladium Nails are fixed to the case.
进一步地，所述链板式高温还原炉设有检修平台、压力监测仪安装孔和温度监测仪安装孔，所述检修平台包括楼梯和检修门，所述链板式高温还原炉通过支架固定在建筑物上。Further, the chain-plate type high-temperature reduction furnace is provided with an inspection platform, a pressure monitor installation hole and a temperature monitor installation hole, the inspection platform includes stairs and an inspection door, and the chain-plate type high-temperature reduction furnace is fixed on the building through brackets. superior.
进一步地，所述盐水蒸发与烟气沉降机自上而下包括高温烟气室、盐水蒸发室和烟气沉降室，所述盐水蒸发室包括两组高温烟气管道和盐水仓，所述高温烟气管道位于盐水仓内，所述高温烟气室上部设有烟气出口、水蒸气出口和烟气进口，所述烟气出口与排风机相连；所述盐水仓侧壁上部设有盐水进口，底部设有浓缩盐水出口，所述浓缩盐水出口与盐水池相连，所述烟气沉降室自上而下包括沉降分离室、集灰斗和出灰口。Further, the brine evaporation and flue gas settling machine includes a high-temperature flue gas chamber, a brine evaporation chamber, and a flue gas settling chamber from top to bottom. The brine evaporation chamber includes two sets of high-temperature flue gas pipes and a brine storehouse. The flue gas pipeline is located in the brine tank, and the upper part of the high-temperature flue gas chamber is provided with a flue gas outlet, a water vapor outlet and a flue gas inlet, and the flue gas outlet is connected with an exhaust fan; the upper part of the side wall of the brine tank is provided with a brine inlet , the bottom is provided with a concentrated brine outlet, the concentrated brine outlet is connected to the brine pool, and the flue gas settling chamber includes a settling separation chamber, ash collecting hopper and ash outlet from top to bottom.
进一步地，所述高温烟气管道每组数量至少为9根，管道厚度为6～12mm，管道直径为20～1000cm，所述高温烟气管道为防止管道积灰还设有压缩空气吹堵机构。Further, the number of each group of the high-temperature flue gas pipes is at least 9, the thickness of the pipes is 6-12 mm, and the diameter of the pipes is 20-1000 cm. The high-temperature flue gas pipes are also equipped with a compressed air blowing mechanism to prevent dust accumulation in the pipes. .
进一步地，所述盐水仓底面设置为向浓缩盐水出口方向倾斜的斜面，其倾斜角度不小于1°。Further, the bottom surface of the brine tank is set as an inclined surface inclined toward the outlet of the concentrated brine, and the inclination angle thereof is not less than 1°.
进一步地，所述高温烟气管道与高温烟气室和烟气沉降室通过法兰连接；所述高温烟气管道与盐水仓通过套管连接，所述套管直径比烟气管大10～20mm，所述套管高度为10～20cm。Further, the high-temperature flue gas pipeline is connected to the high-temperature flue gas chamber and the flue gas settling chamber through flanges; the high-temperature flue gas pipeline is connected to the brine tank through a casing, and the diameter of the casing is 10-10% larger than the flue gas pipe. 20mm, the height of the casing is 10-20cm.
进一步地，所述高温烟气室、烟气沉降室、水蒸气出口、盐水进口、浓缩盐水出口设有温度监测仪、压力监测仪和流量监测仪，所述盐水仓内设有上下料位监测仪，所述温度监测仪、压力监测仪、流量监测仪和上下料位监测仪分别与外设的计算机控制系统相连。Further, the high-temperature flue gas chamber, flue gas settling chamber, water vapor outlet, brine inlet, and concentrated brine outlet are equipped with temperature monitors, pressure monitors, and flow monitors, and the brine tank is equipped with upper and lower material level monitors. The temperature monitor, the pressure monitor, the flow monitor and the upper and lower material level monitors are respectively connected with the peripheral computer control system.
进一步地，所述洗涤脱氯系统包括依次连接的卸料房、板式喂料机、原料储存库、皮带计量秤、皮带输送机、第一除铁器、湿法球磨机、料浆池、第二除铁器、固液分离装置和滤饼储存仓；所述固液分离装置与湿法球磨机相连。Further, the washing and dechlorination system includes sequentially connected unloading room, apron feeder, raw material storage, belt weighing scale, belt conveyor, first iron remover, wet ball mill, slurry tank, second Ironware, a solid-liquid separation device and a filter cake storage bin; the solid-liquid separation device is connected with a wet ball mill.
进一步地，所述原料储存库为密闭圆筒仓，顶部设有进料口，底部设有出料口，所述原料储存库的数量至少2个。Further, the raw material storage is an airtight cylindrical silo, with an inlet at the top and an outlet at the bottom, and there are at least two raw material storages.
进一步地，所述板式喂料机通过提升机与原料储存库进料口相连。Further, the apron feeder is connected to the feed port of the raw material storage through a hoist.
进一步地，所述湿法球磨机为钢球磨机或钢棒磨机。Further, the wet ball mill is a steel ball mill or a steel rod mill.
进一步地，所述固液分离装置为板框压滤机、带式压滤机、浓密机或螺旋过滤机中一种或几种组合。Further, the solid-liquid separation device is one or a combination of plate and frame filter press, belt filter press, thickener or screw filter.
进一步地，所述成球造粒系统包括依次连接的助剂仓、还原剂仓、皮带计量秤、皮带输送机、均质搅拌机和成球机。Further, the pelletizing and granulating system includes an auxiliary agent bin, a reducing agent bin, a belt weighing scale, a belt conveyor, a homogeneous mixer, and a pelletizing machine connected in sequence.
进一步地，所述助剂仓和还原剂仓为密闭圆筒仓，所述助剂仓、还原剂仓与滤饼储存仓底部出料口分别与皮带计量称相连。Further, the auxiliary agent bin and the reducing agent bin are airtight cylindrical bins, and the auxiliary agent bin, the reducing agent bin and the outlet at the bottom of the filter cake storage bin are respectively connected with a belt weighing scale.
进一步地，所述均质搅拌机为双轴搅拌机、轮研机、混凝土搅拌机中一种或几种组合。Further, the homogeneous mixer is one or a combination of twin-shaft mixers, wheel grinders, and concrete mixers.
进一步地，所述造粒机为成球盘、对辊式挤压成球机中一种或两种组合。Further, the granulator is one or a combination of a pelletizer and a pair of roller extrusion pelletizers.
进一步地，所述成球机成球粒径为5～15mm。Further, the particle diameter of the ball forming machine is 5-15 mm.
进一步地，所述烟气处理系统包括依次连接的布袋收尘器、排风机和烟气脱硫氯系统，所述烟气脱硫氯系统包括依次连接的药剂调配池、药剂输送泵和沉降池；所述布袋收尘器为结露耐高温布袋收尘器。Further, the flue gas treatment system includes a bag filter, an exhaust fan, and a flue gas desulfurization and chlorine system connected in sequence, and the flue gas desulfurization and chlorine system includes a chemical preparation tank, a chemical delivery pump, and a settling tank that are connected in sequence; The bag dust collector mentioned above is a condensation and high temperature resistant bag dust collector.
本发明的目的在于提供一种链板式高温还原炉处置钢铁厂收尘灰的方法，包括以下步骤：The object of the present invention is to provide a kind of chain-plate type high-temperature reduction furnace to dispose of the method for iron and steel plant dust collection, comprising the following steps:
S1、洗涤脱氯：将收尘灰磨浸洗涤成粒径小于80um的细粉浆料后进行过滤，得到滤饼和滤液；S1. Washing and dechlorination: filter the dust collection ash into a fine powder slurry with a particle size of less than 80um and obtain a filter cake and filtrate;
S2、成球造粒：将S1得到的滤饼、还原剂和助剂一起配料后制成粒径为5～15mm的料球；S2. Balling and granulation: mix the filter cake obtained in S1, reducing agent and auxiliary agent together to make pellets with a particle size of 5-15 mm;
S3、挥发提锌：将S2制备的料球送入链板式高温还原炉进行高温煅烧，得到固体渣和含铅锌高温烟气；S3. Zinc extraction by volatilization: send the pellets prepared in S2 to a chain-plate high-temperature reduction furnace for high-temperature calcination to obtain solid slag and high-temperature flue gas containing lead and zinc;
S4、烟气处理：将S3得到的含铅锌高温烟氧化处理后得到含有氧化锌和氧化铅固体的高温烟气，通过盐水蒸发与烟气沉降机降温、除尘处理后获得铅锌粉尘和高温烟气，然后再将高温烟气进行脱硫氯净化处理后作为链板式高温还原炉蒸发预热部的烘干热源；烟气从高温链板机高温还原部排出的烟气经过除尘、脱硫氯处理后排放，回收粉尘再经过成球造粒制成料球后再次送入链板式高温还原炉。S4. Flue gas treatment: oxidize the lead-zinc-containing high-temperature smoke obtained in S3 to obtain high-temperature flue gas containing zinc oxide and lead oxide solids, and obtain lead-zinc dust and high-temperature flue gas through salt water evaporation and flue gas settling machine to cool down and dedust. Flue gas, and then desulfurize and purify the high-temperature flue gas as the drying heat source of the evaporation preheating part of the chain plate high-temperature reduction furnace; the flue gas discharged from the high-temperature chain plate machine high-temperature reduction part undergoes dust removal and desulfurization chlorine After discharge, the recovered dust is pelletized to make balls, and then sent to the chain-plate high-temperature reduction furnace again.
本发明的工作原理如下：The working principle of the present invention is as follows:
将钢铁厂收尘灰湿法研磨浸洗涤后制成粒径小于80um的细粉，洗涤脱氯后溶液中的可溶性氯盐进入溶液，将滤饼、还原剂和助剂一起均质搅拌后成球造粒，将物料粒球送入链板式高温还原炉内，进入蒸发预热部的粒球为湿状物，在高温烟气的作用下使水分蒸发。由于是湿状物，不会漏灰，所以蒸发预热部没有设置集灰装置，进入高温还原部的粒球中煤炭在400℃左右高温下开始燃烧，由于本装置采用缺氧燃烧方式，为保证炉内燃烧和还原气氛需要，高温还原部燃料采用高温循环烟气和空气混合助燃，以保证氧含量小于15％，二氧化碳含量高，可以保证缺氧燃烧，煤炭燃烧后产生一氧化碳，高温还原部不会存在氧气，还原部料球内含煤量多，高温条件下(炉内温度大于950℃)，一部分碳和物料接触产生碳热还原，一部分物料与气体中的一氧化碳接触产生气固反应，将锌、铅等氧化物还原为金属，由于金属锌铅的沸点低，在600℃以上为气体，从而进入烟气从高温还原部顶部的烟气出口排出，脱离固体。脱离后的含铅锌高温烟气加入空气后氧化成氧化锌和氧化铅固体，一氧化碳在空气内也完全燃烧，固体粉末并从氧化室下部卸出，高温烟气从氧化室烟气出口出来后进入盐水蒸发与烟气沉降机，蒸发盐水吸收热量使烟气降温，浓缩后盐水进一步处理。从盐水蒸发与烟气沉降机烟气出口出来的高温烟气进入高温静电收尘器净化后通过高温排风机排出后送入链板式高温还原炉用于蒸发预热部蒸发物料粒球。The dust collected from the iron and steel plant is wet ground, soaked and washed to make a fine powder with a particle size of less than 80um. After washing and dechlorination, the soluble chlorine salt in the solution enters the solution, and the filter cake, reducing agent and auxiliary agent are homogeneously stirred together to form a fine powder Ball granulation, the material pellets are sent into the chain-plate type high-temperature reduction furnace, and the pellets entering the evaporation preheating part are wet, and the water is evaporated under the action of high-temperature flue gas. Because it is wet, it will not leak ash, so there is no ash collection device in the evaporation preheating part, and the coal in the pellets entering the high-temperature reduction part starts to burn at a high temperature of about 400 ° C. Since this device adopts an oxygen-deficient combustion method, it is To ensure the combustion and reduction atmosphere in the furnace, the fuel in the high-temperature reduction part uses high-temperature circulating flue gas and air for combustion support to ensure that the oxygen content is less than 15%, and the carbon dioxide content is high, which can ensure anoxic combustion. Carbon monoxide is produced after coal combustion. High-temperature reduction part Oxygen will not exist, and the coal content in the reduction part is large. Under high temperature conditions (the temperature in the furnace is greater than 950 ° C), a part of the carbon contacts with the material to produce carbothermal reduction, and a part of the material contacts with carbon monoxide in the gas to produce a gas-solid reaction. Zinc, lead and other oxides are reduced to metals. Due to the low boiling point of metals, zinc and lead are gases above 600°C, so that the flue gas enters and is discharged from the flue gas outlet at the top of the high-temperature reduction part to separate from solids. The detached high-temperature flue gas containing lead and zinc is oxidized into zinc oxide and lead oxide solids after being added to the air, carbon monoxide is also completely combusted in the air, and the solid powder is discharged from the lower part of the oxidation chamber. After the high-temperature flue gas comes out of the flue gas outlet of the oxidation chamber Entering the brine evaporation and flue gas settling machine, the evaporated brine absorbs heat to cool down the flue gas, and the concentrated brine is further processed. The high-temperature flue gas from the flue gas outlet of the brine evaporation and flue gas settling machine enters the high-temperature electrostatic precipitator for purification, and then is discharged through the high-temperature exhaust fan, and then sent to the chain-plate high-temperature reduction furnace for the evaporation preheating part to evaporate material pellets.
本发明的有益效果如下：The beneficial effects of the present invention are as follows:
(1)本发明针对钢铁厂收尘灰的特性专门设计链板式高温还原炉作为主要火化提炼设备，采用碳热还原方法，还原剂和物料紧密接触，反应速度快，还原效率高，燃烧完全，对收尘灰中的铅锌提取率高，炉渣中残留少。还原反应主要为固态反应，所需烟气量少，因此设备排出的烟气中铅锌浓度高，有利于提高铅锌回收产品的纯度，解决了传统的燃烧方法会在窑内结块影响设备安全运转的隐患。(1) The present invention specially designs chain-plate high-temperature reduction furnace as the main cremation and refining equipment according to the characteristics of dust collection in iron and steel plants. It adopts the carbothermal reduction method, the reducing agent and the material are in close contact, the reaction speed is fast, the reduction efficiency is high, and the combustion is complete. The extraction rate of lead and zinc in dust collection ash is high, and there is little residue in slag. The reduction reaction is mainly a solid-state reaction, and the amount of flue gas required is small. Therefore, the concentration of lead and zinc in the flue gas discharged from the equipment is high, which is conducive to improving the purity of the lead and zinc recovery products, and solves the problem of agglomeration in the kiln that will affect the equipment in the traditional combustion method. hazards to safe operation.
(2)本发明通过科学和系统的方法对钢铁厂收尘灰进行无害化、资源化处理，处理过程中全部在密闭设备和负压环境下操作，并采用高效除尘设备进行处理，没有粉尘污染。发明中可能产生的少量硫和氯等腐蚀性强的酸性气体通过强碱完全可以吸收固化，不会对外排放。(2) The present invention carries out harmless and resourceful treatment of dust collected in iron and steel plants through a scientific and systematic method, all of which are operated in closed equipment and negative pressure environment during the treatment process, and are processed by high-efficiency dust removal equipment, without dust pollute. A small amount of highly corrosive acid gases such as sulfur and chlorine that may be produced in the invention can be completely absorbed and solidified by strong alkali, and will not be discharged externally.
(3)本发明中经过盐水蒸发与烟气沉降机降温后的烟气在收尘处理后也送入链板式高温还原炉用于蒸发预热部蒸发物料粒球；第一次固液分离产生的液体经沉降处理后进行第二次固液分离，产生的液体送入湿法球磨机用作研磨用水，经链板式高温还原炉燃烧后得到的固体渣运输到水泥厂作为铁质校正原料使用或返回钢铁厂作为炼铁原料；处置过程中的废水、废气和废渣可以得到循环使用和有效利用，无二次排放，彻底消除了二次污染的可能。充分利用钢铁厂收尘灰生产高附加值的氧化锌和铁粉，保证钢铁资源不被浪费，创造明显的社会和经济效益。(3) In the present invention, the flue gas after salt water evaporation and flue gas settling machine cooling is also sent to the chain plate type high-temperature reduction furnace after the dust collection treatment to be used for evaporating the preheating part to evaporate material pellets; the first solid-liquid separation produces The second solid-liquid separation is carried out after the liquid is settled, and the resulting liquid is sent to the wet ball mill as grinding water, and the solid slag obtained after being burned in the chain-plate high-temperature reduction furnace is transported to the cement plant for use as iron correction raw material or It is returned to the iron and steel plant as raw material for ironmaking; the waste water, waste gas and waste residue in the disposal process can be recycled and effectively utilized without secondary discharge, completely eliminating the possibility of secondary pollution. Make full use of dust collected by iron and steel plants to produce high value-added zinc oxide and iron powder, to ensure that steel resources are not wasted, and to create obvious social and economic benefits.
(4)本发明中产生的高温含锌铅烟气通过盐水蒸发和烟气沉降系统后，再利用高温静电收尘器方法分离粉尘，与传统的沉降分离方法相比可以有效控制烟气中的含尘量，从而提高了产品纯度。(4) After the high-temperature zinc-lead-containing flue gas produced in the present invention passes through the salt water evaporation and flue gas sedimentation system, the high-temperature electrostatic precipitator method is used to separate the dust, which can effectively control the dust in the flue gas compared with the traditional sedimentation separation method. Dust content, thereby improving product purity.
附图说明Description of drawings
图1为链板式高温还原炉处置钢铁厂收尘灰系统示意图；Figure 1 is a schematic diagram of a chain-plate high-temperature reduction furnace disposal system for collecting dust in a steel plant;
图2为洗涤脱氯系统和成球造粒系统连接示意图；Figure 2 is a schematic diagram of the connection between the washing and dechlorination system and the pelletizing system;
图3为链板式高温还原炉结构示意图；Fig. 3 is a structural schematic diagram of a chain-plate type high-temperature reduction furnace;
图4为高温还原部内部结构示意图；Figure 4 is a schematic diagram of the internal structure of the high temperature reduction section;
图5为机壳构造示意图；Figure 5 is a schematic diagram of the casing structure;
图6为盐水蒸发室与烟气沉降室结构示意图；Fig. 6 is a schematic diagram of the structure of the brine evaporation chamber and the smoke settling chamber;
图7为盐水蒸发室与烟气沉降室俯视图；Figure 7 is a top view of the brine evaporation chamber and the flue gas settling chamber;
上述附图标记：The above reference signs:
101、卸料房；102、板式喂料机；103、原料储存库；104、皮带计量秤；105、皮带输送机；106、第一除铁器；107、湿法球磨机；108、料浆池；109、第二除铁器；110、带式压滤机；111、滤液处理池；112、搅拌罐；113、浓密机；114、板框压滤机；115、滤饼储存仓；101. Unloading room; 102. Plate feeder; 103. Raw material storage; 104. Belt weighing scale; 105. Belt conveyor; 106. First iron remover; 107. Wet ball mill; 108. Slurry pool; 109. Second iron remover; 110. Belt filter press; 111. Filtrate treatment tank; 112. Stirring tank; 113. Thickener; 114. Plate and frame filter press; 115. Filter cake storage bin;
201、助剂仓；202、还原剂仓；203、皮带计量秤；204、皮带输送机；205、均质搅拌机；206、成球机；201. Auxiliary warehouse; 202. Reductant warehouse; 203. Belt weighing scale; 204. Belt conveyor; 205. Homogeneous mixer; 206. Ball forming machine;
301、链板式高温还原炉；302、氧化室；303、盐水蒸发与烟气沉降机；304、高温静电收尘器；305、固体库；306、排风机；307、炉渣库；301. Chain-plate type high-temperature reduction furnace; 302. Oxidation chamber; 303. Salt water evaporation and flue gas settling machine; 304. High-temperature electrostatic precipitator; 305. Solid storage; 306. Exhaust fan; 307. Slag storage;
3011、蒸发预热部；3012、高温还原部；3013、冷却部；3014、烟气室；30141、热烟气进口；3011, evaporation preheating part; 3012, high temperature reduction part; 3013, cooling part; 3014, flue gas chamber; 30141, hot flue gas inlet;
30111、第一进料口；30112、第一烟气出口；30113、第一链板机；30114、第二进料口；30111, the first feed port; 30112, the first flue gas outlet; 30113, the first chain conveyor; 30114, the second feed port;
30121、第二烟气出口；30122、第二链板机；30123、集灰斗；30124、第一出灰口；30125、第三进料口；30126、燃料喷嘴；30127、密封气室；30121, the second flue gas outlet; 30122, the second chain conveyor; 30123, the ash collecting hopper; 30124, the first ash outlet; 30125, the third feeding port; 30126, the fuel nozzle; 30127, the sealing air chamber;
301271、高压空气进气孔；301272、排气孔；301271, high pressure air intake hole; 301272, exhaust hole;
30131、出风口；30132、充气室；30133、第三链板机；30134、出料口；30131, air outlet; 30132, inflatable chamber; 30133, third chain plate machine; 30134, material outlet;
301321、第二出灰口；301322、进风口；301323、隔墙；301321, the second ash outlet; 301322, the air inlet; 301323, the partition wall;
3015、机壳本体；3016、保温材料层；3017、耐火砖层；3018、钯钉；3015, casing body; 3016, insulation material layer; 3017, refractory brick layer; 3018, palladium nails;
3031、高温烟气室；3032、盐水蒸发室；3033、烟气沉降室；3031, high temperature flue gas chamber; 3032, salt water evaporation chamber; 3033, flue gas settling chamber;
30311、烟气出口；30312、水蒸气出口；30313、烟气进口；30311, flue gas outlet; 30312, steam outlet; 30313, flue gas import;
30321、高温烟气管道；30322、盐水仓；30321, high temperature flue gas pipeline; 30322, brine tank;
303221、盐水进口；303222、浓缩盐水出口；303221, salt water import; 303222, concentrated brine export;
30331、沉降分离室；30332、集灰斗；30333、出灰口；30331, settling separation chamber; 30332, ash collecting hopper; 30333, ash outlet;
401、布袋收尘器；402、烟气脱硫氯系统；4021、药剂调配池。401. Bag dust collector; 402. Flue gas desulfurization chlorine system; 4021. Chemical deployment pool.
具体实施方式Detailed ways
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合附图和具体实施例，对本发明进行进一步详细说明。In order to make the object, technical solution and advantages of the present invention clearer, the present invention will be further described in detail below in conjunction with the accompanying drawings and specific embodiments.
如图1-7所示，本实施例提供一种链板式高温还原炉处置钢铁厂收尘灰系统，包括洗涤脱氯系统、成球造粒系统、挥发提锌系统和烟气处理系统；其中洗涤脱氯系统、成球造粒系统和挥发提锌系统依次相连，烟气处理系统与挥发提锌系统相连，系统内的装置均采用密封装置，并设置抽吸机用于形成微负压。As shown in Figures 1-7, this embodiment provides a chain-plate type high-temperature reduction furnace disposal system for dust collection in iron and steel plants, including a washing and dechlorination system, a pelletizing system, a volatile zinc extraction system, and a flue gas treatment system; The washing and dechlorination system, the granulation system and the volatile zinc extraction system are connected in sequence, and the flue gas treatment system is connected with the volatile zinc extraction system. The devices in the system are all sealed devices, and a suction machine is set to form a slight negative pressure.
洗涤脱氯系统包括卸料房101、板式喂料机102、原料储存库103、皮带计量秤104、皮带输送机105、第一除铁器106、湿法球磨机107、料浆池108、第二除铁器109、带式压滤机110、滤液处理池111、搅拌罐112、浓密机113、板框压滤机114和滤饼储存仓115。原料储存103库为密闭圆筒仓，设有3个，可以分别储存高炉灰、电炉灰和转炉灰，原料储存库103顶部设有进料口，底部设有出料口；湿法球磨机107为钢球磨机或钢棒磨机。The washing and dechlorination system includes a discharge room 101, a
成球造粒系统包括依次连接的助剂仓201、还原剂仓202、皮带计量秤203、皮带输送机204、均质搅拌机205和成球机206，其中助剂仓201和还原剂仓202为密闭圆筒仓，助剂仓201、还原剂仓202与滤饼储存仓115底部出料口与皮带计量称203相连，皮带计量称203与皮带输送机204相连。The pelletizing system includes an
优选地，均质搅拌机205选用双轴搅拌机、轮研机、混凝土搅拌机中一种，造粒机206选用成球盘、对辊式挤压成球机中一种，物料球粒径为5～15mm。Preferably, the
挥发提锌系统包括依次连接的链板式高温还原炉301、氧化室302、盐水蒸发与烟气沉降机303、高温静电收尘器304和固体库305，所述高温静电收尘器304通过排风机306与链板式高温还原炉301相连。The volatile zinc extraction system includes a chain-plate high-temperature reduction furnace 301, an oxidation chamber 302, a brine evaporation and flue gas settling machine 303, a high-temperature electrostatic precipitator 304, and a solid storage 305 connected in sequence. The high-temperature electrostatic precipitator 304 passes through the exhaust fan 306 is connected with chain plate type high temperature reduction furnace 301.
链板式高温还原炉301包括炉体和由炉体包裹所形成的空腔，空腔由蒸发预热部3011、高温还原部3012和冷却部3013组成。蒸发预热部3011和冷却部3013设于炉体一侧，高温还原部3012设于炉体另一侧，蒸发预热部3011位于冷却部3013上方，蒸发预热部3011和冷却部3013之间设有烟气室3014，蒸发预热部3011、高温还原部3012和冷却部3013设有链板机，烟气室3014中部设有热烟气进口30141。The chain-plate high-temperature reduction furnace 301 includes a furnace body and a cavity formed by wrapping the furnace body. The cavity is composed of an
蒸发预热部3011上部设有第一进料口30111和第一烟气出口30112，下部设有第一链板机30113，蒸发预热部3011与高温还原部3012的连接处设有第二进料口30114。The upper part of the
高温还原部3012为长方体结构，上部设有第二烟气出口30121，中部设有第二链板机30122，下部设有集灰斗30123，集灰斗30123下部设有第一出灰口30124，其中第一出灰口30124的数量为至少一个，本实施例中设置数量为4个，高温还原部3012与冷却部3013的连接处设有第三进料口30125。The high
优选地，高温还原部3012设有燃料喷嘴30126，数量至少一个，所述燃料喷嘴30126安装于第二链板机30122的上方炉体处。Preferably, the high-
优选地，高温还原部3012第二链板机30122的外部设有密封气室30127，所述密封气室30127为长方体结构，密封气室30127的安装位置为从第二链板机30122的头轮至尾轮处，侧面设有多个高压空气进气孔301271，上部设有至少一个排气孔301272，设置密封气室30127可以对第二链板机30122的链条进行降温，防止第二链板机轴承因为高温而变形。Preferably, a sealed
冷却部3013为上部设有出风口30131，下部设有充气室30132，中部设有第三链板机30133，第三链板机30133物料下落处设有出料口30134，充气室30132底部设有第二出灰口301321，侧壁上设有进风口301322，充气室30132的数量至少一个，不同充气室30132之间设有隔墙301323，作为优选实施方式，本实施例中充气室的数量为3个，每个充气室下部设有至少一个出灰口，第一出灰口30124和第二出灰口301321与炉渣库307相连。The
优选地，蒸发预热部3011、高温还原部3012和冷却部3013第一链板机、第二链板机、第三链板机与炉体顶面的距离为链板机宽度的0.3～1倍，当第一链板机、第二链板机和第三链板机的数量分别为2台或2台以上时，第一链板机与第一链板机之间、第二链板机与第二链板机之间或第三链板机与第三链板机之间的距离为链板机宽度的0.3～1倍，第一链板机、第二链板机和第三链板机上设有耐火材料层，链板机的运行速度为0.01～0.5m/min。。Preferably, the distance between the
其中，链板机为公知技术，包括链板、传动装置、动力装置和张紧装置组成，其中物料的运输主要是通过链条的循环往复运动提供牵引力，以及利用金属板作为输送过程中的承载体引领物料随着水平方向或者倾斜方向输送。Among them, the chain plate machine is a well-known technology, which consists of a chain plate, a transmission device, a power device and a tensioning device. The transportation of materials is mainly to provide traction through the reciprocating motion of the chain, and to use metal plates as the carrier in the conveying process. Lead the material to be conveyed along the horizontal or inclined direction.
优选地，炉体长度≤30m，宽度≤5m。Preferably, the length of the furnace body is ≤30m, and the width is ≤5m.
烟气室靠近高温还原部的一端的机壳，冷却部顶部的机壳与高温还原部靠近烟气室一端的机壳围成一个三角形空间，其中高温还原部的第二链板机尾端裸露在三角形空间内，便于安装第二链板机拉紧装置以及日常检修。The casing at the end of the flue gas chamber close to the high-temperature reduction part, the casing at the top of the cooling part and the casing at the end of the high-temperature reduction part near the flue gas chamber form a triangular space, in which the tail end of the second chain plate machine in the high-temperature reduction part is exposed In the triangular space, it is convenient to install the tensioning device of the second chain conveyor and daily maintenance.
烟气室靠近高温还原部的一端的机壳，冷却部顶部的机壳与高温还原部靠近烟气室一端的机壳围成一个三角形空间，其中高温还原部的第二链板机尾端裸露在三角形空间内，便于安装第二链板机拉紧装置以及日常检修。The casing at the end of the flue gas chamber close to the high-temperature reduction part, the casing at the top of the cooling part and the casing at the end of the high-temperature reduction part near the flue gas chamber form a triangular space, in which the tail end of the second chain plate machine in the high-temperature reduction part is exposed In the triangular space, it is convenient to install the tensioning device of the second chain conveyor and daily maintenance.
炉体的机壳包括钢制机壳本体3015、覆盖在机壳本体上的保温材料层3016和覆盖在保温材料层上的耐火砖层3017，保温材料层与耐火砖层之间设有钯钉3018，具体生产制作时，是在钢制机壳本体上贴加保温材料后再砌筑耐火材料，并根据燃烧物质性能选择耐火材料。The casing of the furnace body includes a
优选地，链板式高温还原炉设有检修平台、压力监测仪安装孔和温度监测仪安装孔，所述检修平台包括楼梯和检修门，所述链板式高温还原炉通过支架固定在建筑物上。Preferably, the chain-plate high-temperature reduction furnace is provided with an inspection platform, a pressure monitor installation hole and a temperature monitor installation hole, the inspection platform includes stairs and an inspection door, and the chain-plate high-temperature reduction furnace is fixed on the building through brackets.
如图6-7所示，盐水蒸发与烟气沉降机303由上而下包括高温烟气室3031、盐水蒸发室3032和烟气沉降室3033，盐水蒸发室3032包括两组高温烟气管道30321和盐水仓30322，高温烟气管道30321位于盐水仓内30322，高温烟气室3031上部设有烟气出口30311、水蒸气出口30312和烟气进口30313，烟气出口30311与排风机相连；盐水仓30322侧壁上部设有盐水进口303221，底部设有浓缩盐水出口303222，其中盐水仓30322底面设置为向浓缩盐水出口303222方向倾斜的斜面，其倾斜角度不小于1°。烟气沉降室3033由上而下包括沉降分离室30331、集灰斗30332和出灰口30333。As shown in Figure 6-7, the brine evaporation and flue gas settling machine 303 includes a high-temperature
其中高温烟气管道30321每组数量至少为9根，管道厚度为6～12mm，管道直径为20～1000cm，高温烟气管道303211为防止管道积灰还设有压缩空气吹堵机构。Among them, the number of high-temperature
高温烟气管道30321与高温烟气室3031和烟气沉降室3033通过法兰连接；所述高温烟气管道30321与盐水仓30322通过套管连接，所述套管直径比烟气管大10～20mm，所述套管高度为10～20cm，其中高温烟气管道30321与高温进出烟气室的连接部，管道内设有耐火材料层，厚度为5～10cm，高温烟气室和烟气沉降室内按常规方式设置有保温材料层和耐火材料层。The high-temperature
高温烟气室3031、烟气沉降室3033、水蒸气出口30312、盐水进口303221、浓缩盐水出口303222设有温度监测仪、压力监测仪和流量监测仪，盐水仓内设有上下料位监测仪，其中温度监测仪、压力监测仪、流量监测仪和上下料位监测仪分别与外设的计算机控制系统相连。The high-temperature
如图1所示，烟气处理系统包括依次连接的布袋收尘器401、排风机和烟气脱硫氯系统402，其中烟气脱硫氯系统402包括依次连接的药剂调配池4021、药剂输送泵和沉降池。As shown in Figure 1, the flue gas treatment system includes a bag filter 401, an exhaust fan, and a flue gas desulfurization and chlorine system 402 connected in sequence, wherein the flue gas desulfurization and chlorine system 402 includes a chemical preparation pool 4021, a chemical delivery pump and Settling tank.
本实施例还提供一种链板式高温还原炉处置钢铁厂收尘灰的方法，其特征在于，包括以下步骤：This embodiment also provides a chain-plate type high-temperature reduction furnace method for disposing of dust collected in iron and steel plants, which is characterized in that it includes the following steps:
S1、洗涤脱氯：将收尘灰磨浸洗涤成粒径小于80um的细粉浆料后进行过滤，得到滤饼和滤液；S1. Washing and dechlorination: filter the dust collection ash into a fine powder slurry with a particle size of less than 80um and obtain a filter cake and filtrate;
S2、成球造粒：将S1得到的滤饼、还原剂和助剂一起配料后制成粒径为5～15mm的料球；S2. Balling and granulation: mix the filter cake obtained in S1, reducing agent and auxiliary agent together to make pellets with a particle size of 5-15 mm;
S3、挥发提锌：将S2制备的料球送入链板式高温还原炉进行高温煅烧，得到固体渣和含铅锌高温烟气；S3. Zinc extraction by volatilization: send the pellets prepared in S2 to a chain-plate high-temperature reduction furnace for high-temperature calcination to obtain solid slag and high-temperature flue gas containing lead and zinc;
S4、烟气处理：将S3得到的含铅锌高温烟氧化处理后得到含有氧化锌和氧化铅固体的高温烟气，通过盐水蒸发与烟气沉降机降温、除尘处理后获得铅锌粉尘和高温烟气，然后再将高温烟气进行脱硫氯净化处理后作为链板式高温还原炉蒸发预热部的烘干热源；烟气从高温链板机高温还原部排出的烟气经过除尘、脱硫氯处理后排放，回收粉尘再经过成球造粒制成料球后再次送入链板式高温还原炉。S4. Flue gas treatment: oxidize the lead-zinc-containing high-temperature smoke obtained in S3 to obtain high-temperature flue gas containing zinc oxide and lead oxide solids, and obtain lead-zinc dust and high-temperature flue gas through salt water evaporation and flue gas settling machine to cool down and dedust. Flue gas, and then desulfurize and purify the high-temperature flue gas as the drying heat source of the evaporation preheating part of the chain plate high-temperature reduction furnace; the flue gas discharged from the high-temperature chain plate machine high-temperature reduction part undergoes dust removal and desulfurization chlorine After discharge, the recovered dust is pelletized to make balls, and then sent to the chain-plate high-temperature reduction furnace again.
本系统的工作过程如下：The working process of this system is as follows:
收尘灰通过专用运输车辆运送至卸料房的进料坑内，通过板式喂料机运送至提升机，通过提升机的作用将收尘灰运送到原料储存库储存，通过收尘灰来源不同设有2个以上原料存储库。将物料通过皮带计量秤称量后，通过第一除铁器去除原料中的铁质，利用皮带输送机运送至湿法球磨机内，同时加入物料量的1-2倍清水一起入磨搅拌、研磨和洗涤，物料中的块状物质被研碎成小于80um细粉。研磨后得到的浆料自动流入料浆池储存，利用泥浆泵将料浆池中的浆料通过第二除铁器继续除掉经过磨细裸露的磁性铁，这些铁质物料与第一除铁器选出的铁质一起返回钢铁厂作为炼钢原料。除铁后的泥浆送入带式压滤机内，过滤得到泥饼和过滤液，过滤液经滤液处理池沉降处理后送入浓密机进行第二次过滤，泥饼送入搅拌罐加入清水后搅拌，搅拌均匀后通过浓密机和板框压滤机进行过滤，经过板框压滤机中过滤后得到滤饼和过滤液，滤饼中含水率20～30％，其中，滤饼送入滤饼储存仓，过滤液返回浓密机中再次利用，此时物料中的可溶性氯盐进入过滤液中，保存于滤液处理池中。The collected dust is transported to the feeding pit of the unloading room by a special transport vehicle, transported to the hoist by the apron feeder, and transported to the raw material storage warehouse by the function of the hoist. There are more than 2 ingredient repositories. After the material is weighed by the belt weighing scale, the iron in the raw material is removed by the first iron remover, and transported to the wet ball mill by a belt conveyor. At the same time, 1-2 times the amount of material is added into the mill for stirring, grinding and grinding. After washing, the bulk material in the material is ground into a fine powder less than 80um. The slurry obtained after grinding automatically flows into the slurry tank for storage, and the slurry in the slurry tank is passed through the second iron remover by a mud pump to continue to remove the finely ground and exposed magnetic iron. These iron materials are separated from the first iron remover. The iron produced is returned to the steel factory together as raw material for steelmaking. The mud after iron removal is sent to the belt filter press, and the mud cake and filtrate are obtained by filtration. The filtrate is settled in the filtrate treatment tank and then sent to the thickener for the second filtration. The mud cake is sent to the mixing tank and added with clean water. Stir, after stirring evenly, filter through a thickener and a plate-and-frame filter press, and obtain filter cake and filtrate after filtering in a plate-and-frame filter press. The moisture content in the filter cake is 20-30%. In the cake storage bin, the filtrate is returned to the thickener for reuse. At this time, the soluble chlorine salt in the material enters the filtrate and is stored in the filtrate treatment tank.
滤饼储存仓通过仓底部出料口的皮带计量称称量，还原剂仓内为固定碳大于78％、粒度小于5mm的焦末或无烟煤，助剂仓内为石灰、石灰石、电石渣、钢渣粉、糖渣、淀粉、谷壳等的一种或几种混合，通过还原剂仓和助剂仓底部出料口的皮带计量称称量后，一起利用皮带输送机运送至均质搅拌机内搅拌，搅拌均匀后送入成球机内制成粒径为5-15mm的粒球。The filter cake storage bin is weighed through the belt meter at the outlet at the bottom of the bin. The reductant bin is filled with coke powder or anthracite with a fixed carbon greater than 78% and a particle size of less than 5mm. The additive bin is filled with lime, limestone, carbide slag, and steel slag. Powder, sugar residue, starch, rice husk, etc., are mixed by belt metering and weighing at the bottom outlet of the reducing agent bin and the auxiliary agent bin, and then transported to the homogeneous mixer by a belt conveyor for mixing. , Stir evenly and send it into the ball forming machine to make pellets with a particle size of 5-15mm.
将粒球从链板式高温还原炉蒸发预热部的第一进料口送入，在第一链板机的运动下，粒球中的水分在下部烟气室的热烟气加热下蒸发，气体从预热蒸发部顶部的烟气出口排出，经过脱水后的含碳料球运动到第一链板机的末端后，通过第二出料口进入到高温还原部。Feed the pellets from the first feeding port of the evaporation preheating part of the chain-plate type high-temperature reduction furnace. Under the movement of the first chain-plate machine, the water in the pellets will be evaporated under the heating of the hot flue gas in the lower flue gas chamber. The gas is discharged from the flue gas outlet at the top of the preheating evaporator, and the dehydrated carbon-containing material balls move to the end of the first chain conveyor, and then enter the high-temperature reduction part through the second outlet.
进入高温还原部的料球在第二链板机的运动下，料球温度进一步升高，为确保高温还原部的温度，通过燃料喷嘴喷入燃料在炉内燃烧产生热量，料球内含煤炭量多，高温条件下(炉内温度为950℃)，一部分物料和碳接触产生碳热还原，一部分物料与气体中的一氧化碳接触产生气固反应，将锌、铅等氧化物还原为金属，由于金属锌铅的沸点低，在600℃以上为气体，因此从进入烟气内，从高温还原部顶部的烟气出口排出，进入氧化室。燃烧后得到的固体炉渣在第二链板机的带动下从第三进料口进入冷却部，燃烧产生的细小炉渣从链板机缝隙漏下，进入灰斗并通过第一出灰口排出。The balls entering the high-temperature reduction part are moved by the second chain plate machine, and the temperature of the balls is further increased. In order to ensure the temperature of the high-temperature reduction part, fuel is injected into the furnace through the fuel nozzle to burn to generate heat. The balls contain coal A large amount, under high temperature conditions (the temperature in the furnace is 950°C), a part of the material contacts with carbon to produce carbothermal reduction, and a part of the material contacts with carbon monoxide in the gas to produce a gas-solid reaction, reducing zinc, lead and other oxides to metals. The boiling point of metal zinc and lead is low, and it is a gas above 600 ° C. Therefore, it enters the flue gas and is discharged from the flue gas outlet at the top of the high-temperature reduction part to enter the oxidation chamber. The solid slag obtained after combustion enters the cooling part from the third feeding port driven by the second chain conveyor, and the fine slag produced by combustion leaks from the gap of the chain conveyor, enters the ash hopper and is discharged through the first ash outlet.
进入冷却部的炉渣在第三链板机的运动下，在底部充气室进入的高压冷空气的作用下进行冷却，此时炉渣中残留的少量未燃烧的碳在空气中进一步燃烧干净，铁和氧化铁均被氧化成三氧化二铁，通过热交换后的高温烟气从冷却室顶部的出风口进入烟气室，作为预热蒸发部的蒸发热源，冷却后的固体渣在第三链板机的带动下从出料口排出，其中细小炉渣从链板机缝隙漏下，进入充气室并通过第二出灰口排出，从第一出灰口、第二出灰口和冷却部出料口排出的固体渣运送到固体渣库保存，运输到水泥厂作为铁质校正原料使用或返回钢铁厂作为炼铁原料。The slag entering the cooling part is cooled under the action of the third chain conveyor and the high-pressure cold air entering the bottom plenum chamber. At this time, a small amount of unburned carbon remaining in the slag is further burned in the air, and the iron and Iron oxide is oxidized to ferric oxide. After heat exchange, the high-temperature flue gas enters the flue gas chamber from the air outlet on the top of the cooling chamber, and is used as the evaporation heat source of the preheating evaporation part. The cooled solid slag is discharged on the third chain plate Driven by the machine, it is discharged from the discharge port, in which the fine slag leaks from the gap of the chain conveyor, enters the air chamber and is discharged through the second ash outlet, and is discharged from the first ash outlet, the second ash outlet and the cooling part The solid slag discharged from the outlet is transported to the solid slag storehouse for storage, transported to the cement plant as iron correction raw material or returned to the steel plant as iron-making raw material.
高温还原部排出的含铅锌高温烟气，其温度大于700℃，进入氧化室内加入空气后氧化成氧化锌和氧化铅固体，同时高温烟气中的一氧化碳也全部燃烧完全，生成的固体从烟气中沉降分离后从氧化室底部排出，送入固体库内储存，而高温含尘烟气通过氧化室烟气出口进入盐水蒸发与烟气沉降机。The high-temperature flue gas containing lead and zinc discharged from the high-temperature reduction part has a temperature greater than 700°C. After entering the oxidation chamber and adding air, it is oxidized into zinc oxide and lead oxide solids. After the gas is settled and separated, it is discharged from the bottom of the oxidation chamber and sent to the solid storage for storage, while the high-temperature dusty flue gas enters the brine evaporation and flue gas settling machine through the flue gas outlet of the oxidation chamber.
高温含尘烟气(1000℃左右)从高温烟气室的烟气进口进入到高温烟气管道内，此时滤液处理池中分离得到的工业盐水通过盐水进口进入盐水仓，经过高温烟气管道的加热使水分蒸发，蒸发后的水蒸气收集备用。降温后的含尘烟气进入底部烟气沉降室，由于气流速度降低，产生固气分离，固体由于重力的作用沉降落到底部集灰斗内，通过出灰口排出，送入固体库内储存。分离后的烟气通过另一组高温烟气管道，同样在盐水降温后，从另一组高温烟气管道顶部的高温烟气室的烟气出口排出，进入高温静电收尘器后除尘后，通过排风机送入链板式高温还原炉内为蒸发预热部提供热量。High-temperature dusty flue gas (about 1000°C) enters the high-temperature flue gas pipeline from the flue gas inlet of the high-temperature flue gas chamber. At this time, the industrial brine separated from the filtrate treatment tank enters the brine tank through the brine inlet, and passes through the high-temperature flue gas pipeline. The heating makes the water evaporate, and the evaporated water vapor is collected for later use. The dust-laden flue gas after cooling enters the bottom flue gas settling chamber, and due to the reduction of the airflow velocity, solid-gas separation occurs, and the solid settles down to the bottom ash collecting hopper due to the action of gravity, and is discharged through the ash outlet, and is sent to the solid storage for storage . The separated flue gas passes through another set of high-temperature flue gas pipes, and after the salt water cools down, it is discharged from the flue gas outlet of the high-temperature flue gas chamber at the top of another set of high-temperature flue gas pipes, and enters the high-temperature electrostatic precipitator for dust removal. It is sent into the chain-plate type high-temperature reduction furnace through the exhaust fan to provide heat for the evaporation preheating part.
盐水仓内蒸发浓缩后的盐水从浓缩盐水出口排出后送入盐水池保存。The evaporated and concentrated brine in the brine tank is discharged from the outlet of the concentrated brine and sent to the brine pool for storage.
从链板式高温还原炉蒸发预热部顶部的烟气出口排出来的烟气利用布袋收尘器净化，布袋收尘器采用抗结露耐高温布袋收尘器，净化后的烟气温度小于100℃，送入烟气脱硫氯系统，其中烟气脱硫氯方法是利用强碱洗涤脱硫氯和石灰沉降。将药剂调配池内的调配好的强碱溶液利用药剂输送泵运送到沉降池沉降池内，反应完成后获得固体为脱硫石膏，可以作为水泥厂原料使用，上层液体为含氯盐水，送入滤液处理池内作为盐水继续循环使用。The flue gas discharged from the flue gas outlet at the top of the evaporation preheating part of the chain-plate high-temperature reduction furnace is purified by a bag filter, which adopts an anti-condensation and high-temperature resistant bag filter, and the temperature of the purified flue gas is less than 100 ℃, sent to the flue gas desulfurization chlorine system, in which the method of flue gas desulfurization chlorine is to use strong alkali to wash desulfurization chlorine and lime sedimentation. The prepared strong alkali solution in the chemical preparation tank is transported to the settling tank by the chemical delivery pump. After the reaction is completed, the solid is desulfurized gypsum, which can be used as a raw material for the cement plant. The upper liquid is chlorine-containing brine, which is sent to the filtrate treatment tank. Continue to recycle as brine.
本发明的工作原理如下：The working principle of the present invention is as follows:
将钢铁厂收尘灰湿法研磨后制成粒径小于80um的细粉，洗涤脱氯后溶液中的可溶性氯盐进入溶液，将滤饼、还原剂和助剂一起均质搅拌后成球造粒，将物料粒球送入链板式高温还原炉内，进入蒸发预热部的粒球为湿状物，在高温烟气的作用下使水分蒸发。由于是湿状物，不会漏灰，所以蒸发预热部没有设置集灰装置，进入高温还原部的粒球中煤炭在400℃左右高温下开始燃烧，由于本装置采用缺氧燃烧方式，为保证炉内燃烧和还原气氛需要，高温还原部燃料采用高温循环烟气和空气混合助燃，以保证氧含量小于15％，二氧化碳含量高，可以保证缺氧燃烧，煤炭燃烧后产生一氧化碳，高温还原部不会存在氧气，还原部料球内含煤量多，高温条件下(炉内温度大于950℃)，一部分碳和物料接触产生碳热还原，一部分物料与气体中的一氧化碳接触产生气固反应，将锌、铅等氧化物还原为金属，由于金属锌铅的沸点低，在600℃以上为气体，从而进入烟气从高温还原部顶部的烟气出口排出，脱离固体。脱粒后的含铅锌高温烟气加入空气后氧化成氧化锌和氧化铅固体，一氧化碳在空气内也完全燃烧，并从氧化室下部卸出，高温烟气从氧化室烟气出口出来后进入盐水蒸发与烟气沉降机，蒸发盐水吸收热量使烟气降温，浓缩后盐水进一步处理。从盐水蒸发与烟气沉降机烟气出口出来的高温烟气进入高温静电收尘器净化后通过高温排风机排出后送入链板式高温还原炉用于蒸发预热部蒸发物料粒球。The dust collected from iron and steel mills is wet-ground to make a fine powder with a particle size of less than 80um. After washing and dechlorination, the soluble chloride salt in the solution enters the solution, and the filter cake, reducing agent and auxiliary agent are homogeneously stirred together and formed into balls. Granules, the material pellets are sent into the chain-plate high-temperature reduction furnace, and the pellets entering the evaporation preheating part are wet, and the water is evaporated under the action of high-temperature flue gas. Because it is wet, it will not leak ash, so there is no ash collection device in the evaporation preheating part, and the coal in the pellets entering the high-temperature reduction part starts to burn at a high temperature of about 400 ° C. Since this device adopts an oxygen-deficient combustion method, it is To ensure the combustion and reduction atmosphere in the furnace, the fuel in the high-temperature reduction part uses high-temperature circulating flue gas and air for combustion support to ensure that the oxygen content is less than 15%, and the carbon dioxide content is high, which can ensure anoxic combustion. Carbon monoxide is produced after coal combustion. High-temperature reduction part Oxygen will not exist, and the coal content in the reduction part is large. Under high temperature conditions (the temperature in the furnace is greater than 950 ° C), a part of the carbon contacts with the material to produce carbothermal reduction, and a part of the material contacts with carbon monoxide in the gas to produce a gas-solid reaction. Zinc, lead and other oxides are reduced to metals. Due to the low boiling point of metals, zinc and lead are gases above 600°C, so that the flue gas enters and is discharged from the flue gas outlet at the top of the high-temperature reduction part to separate from solids. After threshing, the high-temperature flue gas containing lead and zinc is oxidized into zinc oxide and lead oxide solids after being added to the air. Carbon monoxide is also completely burned in the air and discharged from the lower part of the oxidation chamber. The high-temperature flue gas comes out of the flue gas outlet of the oxidation chamber and enters the brine Evaporation and flue gas settling machine, the evaporated brine absorbs heat to cool down the flue gas, and the concentrated brine is further processed. The high-temperature flue gas from the flue gas outlet of the brine evaporation and flue gas settling machine enters the high-temperature electrostatic precipitator for purification, and then is discharged through the high-temperature exhaust fan, and then sent to the chain-plate high-temperature reduction furnace for the evaporation preheating part to evaporate material pellets.
以上内容是结合具体的优选实施方式对本发明所作的进一步详细说明，不能认定本发明的具体实施只限于这些说明。对于本发明所属领域的普通技术人员来说，在不脱离本发明构思的前提下，还可以做出若干简单推演或替换，都应当视为属于本发明的保护范围。The above content is a further detailed description of the present invention in conjunction with specific preferred embodiments, and it cannot be assumed that the specific implementation of the present invention is limited to these descriptions. For those of ordinary skill in the field of the present invention, without departing from the concept of the present invention, some simple deduction or replacement can also be made, which should be regarded as belonging to the protection scope of the present invention.
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Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005068535A (en) * | 2003-08-28 | 2005-03-17 | Jfe Engineering Kk | Method for processing lead or zinc containing gas or fly ash |
| TW200530405A (en) * | 2004-03-03 | 2005-09-16 | Chia-Cheng Wu | Process for recovery of zinc and iron from EAF dust by reduction |
| CN203728902U (en) * | 2014-03-13 | 2014-07-23 | 北京事竟成有色金属研究所 | Integrated solid waste gas ash and zinc-containing ferrovanadium slag recovery device |
| CN106086413A (en) * | 2016-06-16 | 2016-11-09 | 汉中锌业有限责任公司 | A kind of technique of zinc hydrometallurgy lead smelting gas recycling |
| CN106893867A (en) * | 2017-03-10 | 2017-06-27 | 武汉科思瑞迪科技有限公司 | A kind of method that muffle shaft furnace treatment feed powder containing zinc-iron dirt reclaims zinc |
| CN107162084A (en) * | 2017-06-16 | 2017-09-15 | 浙江大学 | A kind of salt water treating system and its method with preposition heat exchanger and rear end deduster |
| EP3323496A1 (en) * | 2016-11-18 | 2018-05-23 | General Electric Technology GmbH | Apparatus and method for reducing acid gas emissions with zero liquid discharge of waste water |
| CN109748526A (en) * | 2019-02-14 | 2019-05-14 | 长沙中硅水泥技术开发有限公司 | A process system and method for co-processing arsenic-alkali slag in a cement kiln |
| CN110131742A (en) * | 2019-06-16 | 2019-08-16 | 清华大学 | Treatment of all components of boiler exhaust smoke and resource recovery method based on waste heat drive |
| CN110512087A (en) * | 2019-09-27 | 2019-11-29 | 广东金宇环境科技有限公司 | A kind of method of high temperature melting furnace processing steel-making dust-collector |
| CN212293697U (en) * | 2020-03-02 | 2021-01-05 | 长沙中硅环保科技有限公司 | Dust collecting system for steel plant disposed by chain plate type high-temperature reduction furnace |
-
2020
- 2020-03-02 CN CN202010134322.0A patent/CN111270077B/en not_active Expired - Fee Related
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005068535A (en) * | 2003-08-28 | 2005-03-17 | Jfe Engineering Kk | Method for processing lead or zinc containing gas or fly ash |
| TW200530405A (en) * | 2004-03-03 | 2005-09-16 | Chia-Cheng Wu | Process for recovery of zinc and iron from EAF dust by reduction |
| CN203728902U (en) * | 2014-03-13 | 2014-07-23 | 北京事竟成有色金属研究所 | Integrated solid waste gas ash and zinc-containing ferrovanadium slag recovery device |
| CN106086413A (en) * | 2016-06-16 | 2016-11-09 | 汉中锌业有限责任公司 | A kind of technique of zinc hydrometallurgy lead smelting gas recycling |
| EP3323496A1 (en) * | 2016-11-18 | 2018-05-23 | General Electric Technology GmbH | Apparatus and method for reducing acid gas emissions with zero liquid discharge of waste water |
| CN106893867A (en) * | 2017-03-10 | 2017-06-27 | 武汉科思瑞迪科技有限公司 | A kind of method that muffle shaft furnace treatment feed powder containing zinc-iron dirt reclaims zinc |
| CN107162084A (en) * | 2017-06-16 | 2017-09-15 | 浙江大学 | A kind of salt water treating system and its method with preposition heat exchanger and rear end deduster |
| CN109748526A (en) * | 2019-02-14 | 2019-05-14 | 长沙中硅水泥技术开发有限公司 | A process system and method for co-processing arsenic-alkali slag in a cement kiln |
| CN110131742A (en) * | 2019-06-16 | 2019-08-16 | 清华大学 | Treatment of all components of boiler exhaust smoke and resource recovery method based on waste heat drive |
| CN110512087A (en) * | 2019-09-27 | 2019-11-29 | 广东金宇环境科技有限公司 | A kind of method of high temperature melting furnace processing steel-making dust-collector |
| CN212293697U (en) * | 2020-03-02 | 2021-01-05 | 长沙中硅环保科技有限公司 | Dust collecting system for steel plant disposed by chain plate type high-temperature reduction furnace |
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